A method for the production of bio-based ethyl acetate

Abstract

The application discloses a kind of production methods of bio-based ethyl acetate, it is related to biomass energy chemical industry field.The method provided in the application comprises: after non-grain biomass raw material is pretreated, it is added to hot fractionation unit, and after deoxidation and volatile fraction, obtain biochar and bio-combustible gas;Bio-combustible gas is added to green energy production unit, and obtain steam and electric energy;Biochar is added to gasification unit, and obtain crude synthesis gas;After refining, crude synthesis gas is added to adsorption separation unit, first purify gas, then separate part carbon monoxide, obtain hydrogen-rich gas;Hydrogen-rich gas is added to synthesis unit, and obtain methanol;Methanol and part carbon monoxide are added to insert carbonyl unit, and obtain unreacted carbon monoxide, unreacted carbon monoxide and acetic acid;Acetic acid and ethanol are added to esterification unit, and obtain unreacted ethanol, unreacted acetic acid and ethyl acetate.The method provided in the application has remarkable economic benefit and environmental benefit.

Description

Technical Field

[0001] This invention relates to the field of biomass energy chemical technology, specifically to a method for producing bio-based ethyl acetate. Background Technology

[0002] With the deepening of the global "dual carbon" strategy, the replacement of fossil resources with renewable resources has become the core direction of the green transformation of the chemical industry. Non-grain biomass, with its advantages of wide availability, abundant reserves, and renewability, has seen its high-value conversion become a key research focus in the industry. The annual output of non-grain biomass such as straw and agricultural and forestry waste is enormous, but traditional disposal methods mostly involve incineration and landfill, which not only cause serious resource waste but also lead to environmental problems such as air pollution and soil erosion. There is an urgent need to develop efficient and clean conversion technologies for the production of chemical products with stable market demand, such as ethyl acetate.

[0003] Ethyl acetate is a versatile green organic solvent widely used in coatings, inks, fragrances, and pharmaceutical intermediates, with consistently stable market demand. Currently, industrial production processes for ethyl acetate are mainly divided into fossil-based and biomass-based routes. The fossil-based route uses ethylene and acetic acid as raw materials, relying on non-renewable petroleum resources, resulting in high carbon emissions and costs significantly affected by international oil price fluctuations, making its economic viability unstable. The biomass-based route produces acetic acid through fermentation, followed by esterification to generate ethyl acetate. However, this route suffers from long fermentation cycles, low efficiency, complex separation processes, and high production costs. Furthermore, some fermentation routes use grains as raw materials, posing a food security risk of competing with humans for food.

[0004] Currently, there is no mature technology for preparing ethyl acetate using biomass gasification. Biomass contains approximately 45% oxygen; direct biomass gasification results in low utilization and carbon conversion rates. Furthermore, the process generates large amounts of tar and moisture, easily causing pipe blockages and equipment corrosion, leading to unstable processes and frequent malfunctions. Therefore, the industry urgently needs a green bio-based ethyl acetate preparation method that avoids the drawbacks of direct biomass gasification, eliminates the inefficiencies of fermentation routes, and achieves efficient, stable, and cost-controllable tiered utilization of non-grain biomass. Summary of the Invention

[0005] The purpose of this invention is to provide a method for producing bio-based ethyl acetate, thereby solving the following technical problems:

[0006] Existing methods for producing ethyl acetate suffer from poor process stability, high costs, and low resource utilization.

[0007] The objective of this invention can be achieved through the following technical solutions:

[0008] A method for producing bio-based ethyl acetate includes at least the following steps:

[0009] After pretreatment of non-grain biomass raw materials, they are added to a thermal fractionation unit. After thermal fractionation to remove oxygen and volatiles, biochar and biocombustible gas are obtained.

[0010] The biogas is added to a green energy production unit to obtain steam and electricity;

[0011] The biochar is added to the gasification unit, and after the gasification reaction, crude syngas is obtained.

[0012] The crude syngas is refined and then added to an adsorption separation unit to purify the gas first, and then separate out some carbon monoxide to obtain hydrogen-rich gas.

[0013] The hydrogen-rich gas is added to the synthesis unit, and after the synthesis reaction, it is purified to obtain methanol.

[0014] The methanol and a portion of the carbon monoxide are added to the carbonyl insertion unit, and after the carbonyl insertion reaction, the mixture is purified to obtain unreacted carbon monoxide, unreacted methanol, and acetic acid.

[0015] The acetic acid and ethanol are added to the esterification unit, and after the esterification reaction, the mixture is purified to obtain unreacted ethanol, unreacted acetic acid, and ethyl acetate.

[0016] As a further aspect of the present invention: the non-grain biomass raw material includes at least straw, agricultural and forestry waste, fermentation residue or kitchen waste, the pretreatment step includes at least impurity removal, crushing and drying, the moisture content of the pretreated non-grain biomass raw material is ≤20%, and the pressure of thermal fractionation deoxygenation and volatile matter removal is 0-0.1MPa and the temperature is 400-700℃.

[0017] As a further aspect of the present invention: the biocombustible gas contains at least carbon monoxide, hydrogen and methane, the calorific value of the biocombustible gas is 2800-4000 Kcal / Nm3, the calorific value of the biochar is 4500-6500 Kcal / Kg, and the temperature of the gasification reaction is 800-120℃ and the pressure is 0.8-1.2 MPa.

[0018] As a further aspect of the present invention: the crude synthesis gas contains at least hydrogen, carbon monoxide and carbon dioxide, and the volume ratio of hydrogen to carbon monoxide in the crude synthesis gas is 1:1; the gasification reaction temperature is 800-1200℃, the pressure is 0.8-1.2MPa, and the gasification medium is crude synthesis gas containing water vapor and oxygen; the refining step includes at least dust removal and desulfurization.

[0019] As a further aspect of the present invention: the purity of the partial carbon monoxide is ≥98.5%, and the partial carbon monoxide accounts for 50% of the volume of carbon monoxide in the crude synthesis gas; the volume concentration of carbon dioxide in the hydrogen-rich gas is ≤0.05%; and the volume ratio of hydrogen to carbon monoxide in the hydrogen-rich gas is 2:1.

[0020] As a further aspect of the present invention: the temperature of the synthesis reaction is 220-280℃, the pressure is 5-10MPa, the catalyst is a copper-based catalyst, and the purity of the methanol is at least 99.5%.

[0021] As a further aspect of the present invention: the molar ratio of methanol to the partial carbon monoxide is 1:1, the temperature of the carbonyl insertion reaction is 170-200℃, the pressure is 3-5MPa, and the catalyst is at least one of a rhodium-based catalyst or an iridium-based catalyst.

[0022] As a further aspect of the present invention: the esterification reaction is carried out at a temperature of 60-75°C, a pressure of 0.1-0.2 MPa, and the catalyst is a sulfonic acid type ion exchange resin catalyst, and the purity of the ethyl acetate is ≥99.5%.

[0023] As a further aspect of the present invention: the unreacted carbon monoxide and the unreacted methanol are returned to the carbonylation unit to participate in the carbonylation reaction, and the unreacted ethanol and the unreacted acetic acid are returned to the esterification unit to participate in the esterification reaction.

[0024] As a further aspect of the present invention, the steam is used at least to meet the heating needs of the thermal fractionation unit, the gasification unit, and the esterification unit.

[0025] The beneficial effects of this invention are:

[0026] This invention provides a method for producing bio-based ethyl acetate. Through biomass thermal fractionation and deoxygenation, the raw material is separated into biochar and biogas, achieving initial deoxygenation and separation of volatiles from the biomass. This solves the persistent problems of tar clogging pipes and corroding equipment in traditional direct gasification processes, significantly improving the continuity and stability of the production process. Simultaneously, this process avoids the drawbacks of traditional biomass-based fermentation routes, such as long cycles, low efficiency, and high costs.

[0027] This invention incorporates a gasification unit and an adsorption separation unit. Through pressure swing adsorption separation, carbon dioxide is directly removed from the crude syngas, and half of the high-purity carbon monoxide in the crude syngas is precisely separated. This process yields hydrogen-rich gas suitable for methanol synthesis and methanol carbonylation reaction in one step. This reduces equipment investment and process complexity caused by water-gas conversion, while avoiding carbon loss and raw material consumption caused by the conversion reaction, thus significantly reducing biomass consumption and overall production costs.

[0028] This invention also incorporates a green energy production unit, achieving efficient tiered utilization of non-grain biomass resources and energy self-sufficiency. Biogas, after purification, is used for tiered energy supply, prioritizing the thermal fractionation unit's needs, with the remainder used for power generation or steam supply to the entire process. Energy self-sufficiency exceeds 75%, significantly reducing dependence on external fossil fuels. Simultaneously, both the carbonylation and esterification units are equipped with raw material recycling systems, ensuring the complete recovery and reuse of unreacted raw materials. Combined with precise process control, the total utilization rate of non-grain biomass raw materials is ≥98%, constructing a closed-loop production system that synergizes resources and energy.

[0029] The production process provided by this invention is widely adaptable and highly controllable, capable of processing various non-grain biomass raw materials such as straw, agricultural and forestry waste, fermentation residue, and kitchen waste. The entire process achieves continuous production, with process parameters collected and automatically adjusted in real time through an online monitoring system. The purity of the product, ethyl acetate, is consistently ≥99.5%. The production process involves no highly corrosive or toxic additives, resulting in low equipment maintenance costs and strong process stability, demonstrating excellent prospects for industrial-scale promotion. This invention's production process completely replaces fossil resources such as petroleum and coal with renewable non-grain biomass as raw materials, significantly reducing carbon emissions at the source. Simultaneously, the production process incorporates environmental protection steps such as dust removal, desulfurization, and decarbonization, significantly reducing emissions of pollutants such as sulfides, dust, and carbon dioxide. This aligns with the "dual-carbon" strategy and the development trend of green chemistry, offering significant environmental and social benefits. Attached Figure Description

[0030] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, for those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0031] Figure 1 This is a process flow diagram of a method for producing bio-based ethyl acetate in one embodiment. Detailed Implementation

[0032] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0033] Please see Figure 1As shown, this invention provides a method for producing bio-based ethyl acetate, comprising at least a thermal fractionation unit, a gasification unit, an adsorption separation unit, a synthesis unit, a carbonylation unit, an esterification unit, and a green energy production unit. The specific steps of the method for producing bio-based ethyl acetate are as follows:

[0034] Please see Figure 1 As shown, non-grain biomass raw materials undergo pretreatment. In one embodiment of the invention, the non-grain biomass raw materials include at least straw, agricultural and forestry waste, fermentation residue, or kitchen waste. Pretreatment includes, for example, at least impurity removal, crushing, and dehydration. The raw materials are crushed to a particle size of less than 50 mm and dehydrated to a moisture content of less than 20% to remove impurities and optimize the thermal fractionation deoxygenation and volatile matter removal effects. After pretreatment, the raw materials are fed into a thermal fractionation unit for thermal fractionation deoxygenation and volatile matter removal to obtain biochar and biocombustible gas. In one embodiment of the invention, the pressure for thermal fractionation deoxygenation and volatile matter removal is, for example, 0-0.1 MPa, and the temperature is, for example, 400-700°C. In one embodiment of the invention, the main components (by volume) of the biocombustible gas are, for example, 25-30% carbon monoxide, 30-35% hydrogen, and 10-20% methane, and the calorific value of the biocombustible gas is, for example, 2800-4000 Kcal / Nm³. 3 Biogas is added to the green energy production unit. A portion of the biogas is used to drive power generation, providing electricity for all units in the process. The remaining biogas is burned to produce steam, providing heat for units requiring heating. This steam is first used to power the thermal fractionation unit, with the remainder powering other units. Any energy shortage is supplemented by external clean energy sources. In one embodiment of the invention, biochar is transported to the next production unit, and the calorific value of the biochar is, for example, 4500-6500 kcal / kg.

[0035] Please see Figure 1 As shown, the biochar obtained from the thermal fractionation unit is fed into the gasification unit for gasification to obtain crude syngas. In one embodiment of the invention, the biochar particle size is less than 1 mm, the gasification temperature is, for example, 800-1200°C, the pressure is 0.8-1.2 MPa, and the gasification medium is, for example, crude syngas composed of oxygen and water vapor. The main components of the generated crude syngas are carbon monoxide, hydrogen, and a small amount of carbon dioxide. In one embodiment of the invention, the volume ratio of carbon monoxide to hydrogen in the crude syngas is, for example, 1:1. In this invention, the obtained crude syngas is refined before being added to the next production unit. In one embodiment of the invention, the refining process includes, for example, dust removal and desulfurization to remove impurities that affect subsequent separation and reaction.

[0036] Please see Figure 1As shown, the refined crude syngas is fed into an adsorption separation unit. The gas is first purified by pressure swing adsorption (PSA) separation, and then a portion of carbon monoxide is separated to obtain hydrogen-rich gas. In one embodiment of the invention, the gas purification step includes, for example, at least the removal of carbon dioxide. The separated portion of carbon monoxide accounts for 50% of the volume of carbon monoxide in the crude syngas, and the purity of the separated portion of carbon monoxide is, for example, not less than 98.5%. The volume concentration of carbon dioxide in the hydrogen-rich gas obtained after the adsorption separation unit is, for example, not more than 0.05%, and the volume ratio of hydrogen to carbon monoxide in the hydrogen-rich gas is 2:1.

[0037] Please see Figure 1 As shown, the hydrogen-rich gas obtained after adsorption separation does not require additional carbon dioxide supplementation and directly meets the reaction requirement of a hydrogen to carbon monoxide molar ratio of 2:1. It is then directly fed into the synthesis unit for synthesis reaction. After purification, methanol is obtained. In one embodiment of the invention, the synthesis reaction temperature is, for example, 220-280°C, the pressure is, for example, 5-7 MPa, the catalyst is, for example, a copper-based catalyst, and the purity of the purified methanol is, for example, not less than 99.5%.

[0038] Please see Figure 1 As shown, methanol obtained from the synthesis unit and a portion of carbon monoxide separated from the adsorption separation unit are fed into the carbonylation unit for a carbonylation reaction to obtain a mixed product containing acetic acid. This mixed product is then purified to obtain acetic acid, unreacted methanol, and unreacted carbon monoxide with a purity of at least 98.5%. In one embodiment of the invention, the molar ratio of the carbon monoxide and dimethyl ether added to the carbonylation unit is, for example, 1:1. The temperature of the carbonylation reaction is, for example, 260-280°C, the pressure is, for example, 4-6 MPa, and the catalyst is, for example, a rhodium-based or iridium-based catalyst. In one embodiment of the invention, the carbonylation unit is also equipped with a raw material recycling system, allowing the unreacted methanol and unreacted carbon monoxide obtained after purification of the acetic acid-containing mixed product to be returned to the carbonylation unit for re-participation in the carbonylation reaction.

[0039] Please see Figure 1 As shown, ethanol and acetic acid obtained after carbonylation reaction and purification are added to an esterification unit for esterification to obtain an esterification product. The esterification product is then purified to obtain ethyl acetate with a purity of at least 99.5%, unreacted ethanol, and unreacted acetic acid. In one embodiment of the invention, the esterification reaction temperature is, for example, 60-75°C, the pressure is, for example, 0.1-0.2 MPa, and the catalyst is, for example, a sulfonic acid-type ion exchange resin. In one embodiment of the invention, the esterification unit is also equipped with a raw material recycling system, allowing the unreacted ethanol and unreacted acetic acid obtained after purification of the esterification product to be returned to the esterification unit for re-participation in the esterification reaction.

[0040] This invention provides a method for producing bio-based ethyl acetate. Material transportation in each step is achieved through pipelines and pumps to form a continuous production process. The specific operating parameters of each unit are automatically controlled by an online monitoring system, and the total utilization rate of raw materials is not less than 98%.

[0041] The method for producing bio-based ethyl acetate in this example includes the following steps:

[0042] like Figure 1 As shown, 1000 kg of corn stalks were selected as non-grain biomass raw material. After pretreatment to remove impurities such as soil and stones, the stalks were crushed into granular material with a particle size of 30-50 mm. This granular material was then dried at 120℃ until the moisture content dropped to 15% before being fed into the thermal fractionation unit. The thermal fractionation unit was a continuous thermal fractionation reactor, which carried out atmospheric pressure thermal fractionation deoxygenation and volatile matter removal at 0.05 MPa and 500℃ for 2 hours, ultimately yielding 220 kg of biochar and 180 Nm³ of biomass. 3 Biogas. The biochar has a calorific value of 4800 kcal / kg. After being ground to a particle size of 0.8 mm, it is fed into the gasification unit, where the biogas has a calorific value of 3200 kcal / Nm³. 3 It is then fed into the green energy production unit.

[0043] like Figure 1 As shown, the biogas is purified by tar removal and dust removal before being sent to the green energy production unit. The main components (by volume) of the biogas are 28% carbon monoxide, 32% hydrogen, and 15% methane, with the remainder being inert gases. The purified biogas is then sent to the green energy production unit for tiered utilization, with priority given to allocating 80 Nm³ of fuel. 3 The combustion of biogas produces steam, which is used to heat the thermal fractionation unit, meeting the temperature requirements of the thermal fractionation reactor (40 Nm³). 3 The combustion process generates 1.0 MPa saturated steam, which supplies the heating needs of gasification, esterification, and other process units, with a remaining 60 Nm³ of steam. 3 Biogas is fed into a gas turbine generator set to generate electricity, providing power to all units throughout the entire process, including pretreatment, drying, grinding, and refining. Calculations show that in this embodiment, biogas can meet 75% of the energy demand for the entire process, with the remaining 25% energy gap supplemented by wind power generation (external clean energy), ensuring stable operation of all units.

[0044] like Figure 1 As shown, the 220 kg of biochar was fed into a gasification unit for gasification. After purification, crude syngas was obtained. The gasification unit was a fixed-bed gasification reactor, with the gasification temperature controlled at 1000℃ and the gasification pressure at 1 MPa. Oxygen-water vapor (volume ratio 1:2.5) was used as the gasification medium to obtain 350 Nm³ of syngas.3 The crude syngas contains hydrogen and carbon monoxide in a 1:1 volume ratio, as well as 5% carbon dioxide by volume, and trace amounts of sulfides and dust impurities.

[0045] like Figure 1 As shown, the crude syngas is sequentially passed through a dust removal device to remove dust and impurities, and a desulfurization tower to remove sulfides, completing the refining process. It is then sent to an adsorption separation unit, where pressure swing adsorption (PSA) is used to purify the gas, removing carbon dioxide from the crude syngas. The volume concentration of carbon dioxide in the remaining gas is reduced to 0.03%. Further PSA is then used to separate some carbon monoxide, yielding a 175 Nm³ syngas. 3 Hydrogen-rich gas. The separated carbon monoxide accounts for 50% of the total carbon monoxide volume in the crude syngas, and the separated carbon monoxide has a purity of 99.2% and a volume of 87.5 Nm³. 3 The volume ratio of hydrogen to carbon monoxide in the hydrogen-rich gas is 2:1.

[0046] like Figure 1 As shown, the hydrogen-rich gas obtained from the adsorption separation unit does not require additional carbon dioxide supplementation and directly meets the reaction requirement of a 2:1 molar ratio of hydrogen to carbon monoxide, and is directly fed into the synthesis unit for the synthesis reaction. The synthesis unit is a methanol synthesis reactor, which is filled with a copper-based catalyst (Cu-Zn-Al catalyst). The reaction temperature is controlled at 265℃ and the reaction pressure at 6.0MPa to carry out the methanol synthesis reaction. After the reaction is completed, it is purified by a purification tower to obtain 92kg of methanol with a purity of 99.8%.

[0047] like Figure 1 As shown, the 87.5 Nm separated by the above adsorption separation unit 3 A portion of carbon monoxide with a purity of 99.2% was fed into a carbonylation unit with 92 kg of purified methanol with a purity of 99.8% to undergo a carbonylation reaction. The carbonylation unit was a methanol carbonylation reactor, packed with a rhodium-based catalyst. The reaction temperature was controlled at 185℃ and the reaction pressure at 4.5 MPa to produce a mixed product containing acetic acid. After the reaction was completed, the acetic acid-containing mixed product was purified to obtain 8.5 Nm 3 Unreacted carbon monoxide, 7.8 kg of unreacted methanol, and 115 kg of acetic acid with a purity of 99.0% were disposed of. The unreacted carbon monoxide and unreacted methanol were recycled back to the carbonyl insertion unit for reuse.

[0048] like Figure 1As shown, 70 kg of ethanol introduced from outside the boundary area and 115 kg of purified acetic acid were mixed and fed into the esterification unit, which was an esterification reactor. The esterification reactor was filled with a sulfonic acid-type ion exchange resin catalyst, and the reaction temperature was controlled at 68°C and the reaction pressure at 0.15 MPa to carry out the esterification reaction to produce ethyl acetate. After the reaction was completed, it was purified to obtain 6.2 kg of unreacted acetic acid, 4.5 kg of unreacted ethanol, and 142 kg of ethyl acetate with a purity of 99.7%. The unreacted acetic acid and unreacted ethanol were recovered and returned to the esterification unit for recycling.

[0049] In this embodiment, the various units are linked through dedicated pipelines, pumps, and conveyors to achieve continuous production throughout the entire process. Process parameters such as reaction temperature, pressure, and flow rate in each unit are collected in real time and automatically controlled via an online monitoring system to ensure process stability. Using the bio-based ethyl acetate production method provided in the above embodiment, 1000 kg of corn stalk raw material ultimately yields 142 kg of ethyl acetate product, achieving a total raw material utilization rate of 98.3% (≥98%) and an energy self-sufficiency rate of 75%. This effectively overcomes the shortcomings of low efficiency in traditional fermentation routes and easy coking in gasification routes, realizing the efficient and green conversion of non-grain biomass.

[0050] In the description of this specification, references to terms such as "an embodiment," "example," "specific example," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the invention. In this specification, illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples.

[0051] The foregoing has provided a detailed description of one embodiment of the present invention, but this description is merely a preferred embodiment and should not be construed as limiting the scope of the invention. All equivalent variations and modifications made within the scope of the claims of this invention should still fall within the patent coverage of this invention.

Claims

1. A method for producing bio-based ethyl acetate, characterized in that, At least the following steps are included: After pretreatment of non-grain biomass raw materials, they are added to a thermal fractionation unit. After thermal fractionation to remove oxygen and volatiles, biochar and biocombustible gas are obtained. The biogas is added to a green energy production unit to obtain steam and electricity; The biochar is added to the gasification unit, and after the gasification reaction, crude syngas is obtained. The crude syngas is refined and then added to an adsorption separation unit to purify the gas first, and then separate out some carbon monoxide to obtain hydrogen-rich gas. The hydrogen-rich gas is added to the synthesis unit, and after the synthesis reaction, it is purified to obtain methanol. The methanol and a portion of the carbon monoxide are added to the carbonyl insertion unit, and after the carbonyl insertion reaction, the mixture is purified to obtain unreacted carbon monoxide, unreacted methanol, and acetic acid. The acetic acid and ethanol are added to the esterification unit, and after the esterification reaction, the mixture is purified to obtain unreacted ethanol, unreacted acetic acid, and ethyl acetate.

2. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The non-grain biomass raw materials include at least straw, agricultural and forestry waste, fermentation residue or kitchen waste, and the pretreatment steps include at least impurity removal, crushing and drying. The moisture content of the pretreated non-grain biomass raw materials is ≤20%, and the pressure of thermal fractionation deoxygenation and volatile matter removal is 0-0.1 MPa and the temperature is 400-700℃.

3. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The biogas contains at least carbon monoxide, hydrogen, and methane, and the calorific value of the biogas is 2800-4000 kcal / Nm³. 3 The biochar has a calorific value of 4500-6500 Kcal / Kg, and the gasification reaction is carried out at a temperature of 800-120℃ and a pressure of 0.8-1.2 MPa.

4. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The crude synthesis gas contains at least hydrogen, carbon monoxide, and carbon dioxide, and the volume ratio of hydrogen to carbon monoxide in the crude synthesis gas is 1:

1. The gasification reaction is carried out at a temperature of 800-1200℃ and a pressure of 0.8-1.2MPa. The gasification medium is crude synthesis gas containing water vapor and oxygen. The refining steps include at least dust removal and desulfurization.

5. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The purity of the carbon monoxide is ≥98.5%, and the carbon monoxide accounts for 50% of the volume of carbon monoxide in the crude synthesis gas. The volume concentration of carbon dioxide in the hydrogen-rich gas is ≤0.05%, and the volume ratio of hydrogen to carbon monoxide in the hydrogen-rich gas is 2:

1.

6. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The synthesis reaction is carried out at a temperature of 220-280℃, a pressure of 5-10MPa, and a copper-based catalyst. The purity of the methanol is at least 99.5%.

7. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The molar ratio of methanol to carbon monoxide is 1:1, the temperature of the carbonyl insertion reaction is 170-200℃, the pressure is 3-5MPa, and the catalyst is at least one of rhodium-based or iridium-based catalysts.

8. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The esterification reaction is carried out at a temperature of 60-75℃ and a pressure of 0.1-0.2MPa, using a sulfonic acid-type ion exchange resin catalyst, and the ethyl acetate has a purity of ≥99.5%.

9. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The unreacted carbon monoxide and unreacted methanol are returned to the carbonylation unit to participate in the carbonylation reaction, and the unreacted ethanol and unreacted acetic acid are returned to the esterification unit to participate in the esterification reaction.

10. The method for producing bio-based ethyl acetate according to claim 1, characterized in that, The steam is used at least to meet the heating needs of the thermal fractionation unit, the gasification unit, and the esterification unit.

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