Product extraction device for producing acetone through synthesis gas pressure fermentation

Abstract

The utility model relates to a product extraction device for producing acetone through synthesis gas pressure fermentation, which comprises a synthesis gas pressure fermentation tank, a membrane filtration unit, a reduced pressure flash tank, a gas condensation pipe and an acetone storage tank, a liquid inlet of the membrane filtration unit is communicated with a fermentation liquid discharge port, and a reflux inlet of the membrane filtration unit is communicated with the fermentation tank; a liquid inlet of the reduced-pressure flash evaporation pipe is communicated with a liquid outlet of the membrane filtration unit; a gas inlet of the gas condensation pipe is communicated with a vapor phase outlet of the vacuum flash tank; and a condensate outlet of the gas condensation pipe is communicated with an acetone storage tank. According to the product extraction device, firstly, thalli of fermentation liquor are intercepted through the membrane filtration unit, the activity of the thalli is reserved, and the influence on the activity of the thalli is low; according to the invention, acetone is used as a raw material, then the reduced pressure flash tank is used for reducing the pressure of the fermentation liquid and then flash evaporation is carried out, the temperature is maintained at 60 DEG C by using fermentation waste heat, so that the acetone is rapidly vaporized to form gas-liquid two-phase flow, and the design not only improves the vaporization efficiency of the acetone, but also reduces the additional cooling requirement and reduces the energy consumption.

Description

Technical Field

[0001] This utility model relates to the field of acetone fermentation technology, and in particular to a product extraction device for producing acetone by syngas pressure fermentation. Background Technology

[0002] In recent years, syngas fermentation technology has attracted attention as an emerging bio-fermentation method. This technology utilizes autotrophic microorganisms to convert syngas (mainly composed of carbon monoxide, carbon dioxide, and hydrogen) into chemicals such as acetone via the Wood-Ljungdahl pathway. Although syngas fermentation has advantages such as a wide range of raw material sources and the ability to achieve carbon recycling, it still faces some challenges in practical applications. For example, the gas transport efficiency during fermentation is relatively low, resulting in insufficient utilization of syngas by microorganisms; at the same time, the concentration of fermentation products is low, requiring further optimization of fermentation conditions and strain performance.

[0003] In the syngas fermentation process for acetone production, pressurization is a key measure to improve fermentation efficiency and product concentration. Syngas (mainly composed of CO, H2, and CO2) has low solubility under normal pressure, making it difficult to meet the substrate concentration requirements for microbial metabolism, thus limiting fermentation efficiency. Pressurization significantly increases the solubility of syngas in the fermentation broth, allowing more gaseous substrate to enter the fermentation system, providing sufficient carbon and energy sources for microorganisms. Pressurization also accelerates the movement of gas molecules, enhancing the contact between the gas and the microbial cell surface, thereby improving mass transfer efficiency and enabling faster gas utilization by microorganisms. This not only increases acetone yield and production efficiency but may also shorten the fermentation cycle and reduce production costs. Furthermore, pressurized fermentation reduces gas escape from the fermentation broth, making the fermentation process more stable and contributing to the stability and consistency of the fermentation system. Although pressurized fermentation requires pressure-resistant equipment and consumes additional energy, its advantages in improving fermentation efficiency, product concentration, and process stability make it an indispensable key technology in the syngas fermentation process for acetone production.

[0004] The acetone concentration in syngas fermentation broth is typically below 5%, and it coexists with byproducts such as isopropanol, ethanol, and organic acids, forming a highly diluted and complex mixture. Traditional distillation methods are energy-intensive due to the high water content (requiring the evaporation of large amounts of water), making them uneconomical. Furthermore, maintaining cell activity is crucial during the separation process in thermophilic fermentation systems; conventional solid-liquid separation techniques (such as centrifugation and filtration) can easily lead to cell loss or metabolic inhibition. While pressurized fermentation processes (e.g., 0.7 MPa) can increase the reaction rate, the boiling point of acetone rises above 130°C with increasing pressure, making gas phase recovery difficult. Utility Model Content

[0005] Therefore, it is necessary to provide a product extraction device for acetone production by syngas pressure fermentation with relatively low energy consumption, low cost, minimal impact on cell activity during separation, and applicability to pressure fermentation processes.

[0006] This application provides a product extraction apparatus for acetone production via syngas pressure fermentation, comprising:

[0007] A syngas pressurized fermenter, wherein the syngas pressurized fermenter is used to produce acetone based on syngas fermentation, and the syngas pressurized fermenter has a fermentation broth outlet;

[0008] A membrane filtration unit is provided with a filter membrane for retaining bacterial cells. The membrane filtration unit has an inlet, an outlet, and a reflux port. The inlet of the membrane filtration unit is connected to the fermentation broth outlet, and the reflux port of the membrane filtration unit is connected to the fermentation tank.

[0009] A vacuum flash evaporator has a liquid inlet, a vapor phase outlet and a liquid phase outlet, and the liquid inlet of the vacuum flash evaporator tube is connected to the liquid outlet of the membrane filtration unit.

[0010] A gas condenser has an inlet, a condensate outlet, and a gas outlet, and the inlet of the gas condenser is connected to the vapor phase outlet of the vacuum flash tank.

[0011] An acetone storage tank, wherein the condensate outlet of the gas condenser is connected to the acetone storage tank;

[0012] An adsorption tower having a corresponding inlet and outlet, the adsorption tower being filled with adsorption particles for adsorbing acetone, and the inlet of the adsorption tower being connected to the gas outlet of the gas condenser.

[0013] In one embodiment, the liquid phase outlet of the reduced pressure flash evaporator is connected to the syngas pressurized fermenter.

[0014] In one embodiment, the product extraction device further includes a circulation pump and a pressurization module, and the liquid phase outlet of the vacuum flash tank is connected to the syngas pressurized fermenter through the circulation pump and the pressurization module.

[0015] In one embodiment, the membrane filtration unit is a ceramic membrane filtration unit, which is provided with a ceramic filter membrane that traps bacteria.

[0016] In one embodiment, the ceramic filter membrane has a pore size of 0.1–0.2 μm.

[0017] In one embodiment, the gas condenser is a stepped-temperature gas condenser.

[0018] In one embodiment, the gas condenser includes a primary condenser and a secondary condenser connected in sequence. The temperature of the cooling medium in the primary condenser is higher than the temperature of the cooling medium in the secondary condenser. The condensate outlets of the primary condenser and the secondary condenser are both connected to the acetone storage tank.

[0019] In one embodiment, the adsorption tower is an activated carbon adsorption tower, which is filled with activated carbon.

[0020] In one embodiment, the pressure-reducing flash tank is equipped with a pressure-reducing valve for adjusting the pressure reduction opening.

[0021] In one embodiment, the product extraction apparatus further includes a short-path distillation column connected to the acetone storage tank, the short-path distillation column being used to distill and purify the crude acetone in the acetone storage tank.

[0022] The aforementioned acetone extraction apparatus for syngas pressure fermentation addresses the challenge of difficult gas-phase recovery caused by acetone boiling points exceeding 130°C during pressurized fermentation processes (e.g., 0.7 MPa). Firstly, a membrane filtration unit retains the fermentation broth cells, preserving their activity with minimal impact. Then, a vacuum flash evaporator depressurizes the fermentation broth before flash evaporation, utilizing residual heat to maintain a temperature of 60°C, enabling rapid acetone vaporization and forming a gas-liquid two-phase flow. This design not only improves acetone vaporization efficiency but also reduces additional cooling requirements and energy consumption. A condenser is then used to condense the acetone in the vapor, followed by adsorption to recover the uncondensed acetone, ensuring an acetone recovery rate of over 99.5% in the fermentation product. Compared to traditional distillation methods, this approach, through depressurization, condensation, and adsorption, offers relatively lower energy consumption, lower costs, and easier recovery. In other preferred embodiments, energy costs can be further reduced by using stepped temperature condensation through a primary condenser and a secondary condenser. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the product extraction device for producing acetone by syngas pressure fermentation according to an embodiment of the present invention. Detailed Implementation

[0024] To facilitate understanding of this utility model and to make the aforementioned objects, features, and advantages of this utility model more apparent, the specific embodiments of this utility model are described in detail below with reference to the accompanying drawings. Many specific details are set forth in the following description to provide a thorough understanding of this utility model, and preferred embodiments are shown in the accompanying drawings. However, this utility model can be implemented in many different forms and is not limited to the embodiments described herein. Rather, these embodiments are provided to provide a more thorough and complete understanding of the disclosure of this utility model. This utility model can be implemented in many other ways different from those described herein, and those skilled in the art can make similar modifications without departing from the spirit of this utility model; therefore, this utility model is not limited to the specific embodiments disclosed below. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this utility model pertains. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the utility model. The term “and / or” as used herein includes any and all combinations of one or more of the related listed items.

[0025] This application provides a product extraction apparatus for acetone production via syngas pressure fermentation. Please refer to [link to apparatus]. Figure 1 The product extraction device includes: a syngas pressurized fermenter 100, a membrane filtration unit 200, a vacuum flash evaporator 300, a gas condenser 400, an acetone storage tank 500, and an adsorption tower 600.

[0026] The syngas pressurized fermenter 100 is used to produce acetone based on syngas fermentation. The syngas pressurized fermenter 100 has a fermentation broth outlet. Syngas fermentation utilizes autotrophic microorganisms to convert syngas (mainly composed of carbon monoxide, carbon dioxide, and hydrogen) into acetone and other chemicals via the Wood-Ljungdahl pathway. For example, *Moorella thermoacetica* is typically selected as the microbial cell, which has the characteristic of producing acetone by fermenting CO2 and H2 at 60°C. It should be noted that how to prepare acetone from syngas based on *Moorella thermoacetica* can be referred to in previous patents of the applicant and related parties, and will not be elaborated upon here. During syngas fermentation, although pressurized fermentation (e.g., 0.7 MPa) can increase the reaction rate, it raises the boiling point of acetone to above 130°C under pressure, making it difficult for acetone to volatilize at the fermentation temperature of 60°C. The syngas pressurized fermenter mentioned in this application is a syngas fermenter for producing acetone through a pressurized fermentation process (e.g., 0.7 MPa).

[0027] In this application, the membrane filtration unit 200 is equipped with a filter membrane that traps bacterial cells. The membrane filtration unit has an inlet, an outlet, and a reflux port. The inlet of the membrane filtration unit is connected to the fermentation broth outlet, and the reflux port is connected to the fermenter. The membrane filtration unit 200 ensures the passage of fermentation broth through the filter membrane, but the bacterial cells are trapped by the membrane. The trapped bacterial broth can be returned to the fermenter. For example, the membrane filtration unit is a ceramic membrane filtration unit, equipped with a ceramic filter membrane that traps bacterial cells. For example, the pore size of the ceramic filter membrane is 0.1–0.2 μm. Alternatively, the ceramic filter membrane can be a high-temperature resistant ceramic filter membrane. In this application, the trapped clarified fermentation broth enters a vacuum flash evaporator. For example, the operating pressure of the membrane filtration unit 200 is 0.65–0.7 MPa (to avoid membrane fouling), and the membrane flux is 50–100 L / (m³). 2 •h), bacterial cell retention rate: ≥99%.

[0028] A vacuum flash evaporator 300 is used to flash-evaporate fermentation broth after depressurization. The vacuum flash evaporator 300 has a liquid inlet, a vapor phase outlet, and a liquid phase outlet. The liquid inlet of the vacuum flash evaporation tube is connected to the liquid outlet of the membrane filtration unit. In this application, to reduce energy consumption and control costs, the fermentation temperature of the broth (approximately 60°C) is utilized. By reducing the pressure of the fermentation broth to micro-pressure or atmospheric pressure, acetone volatilization can be achieved based on the temperature of the fermentation broth itself. For example, when the fermentation broth is depressurized from 0.7 MPa to atmospheric pressure (0.1 MPa), the boiling point of acetone drops from 130°C to 56.5°C, rapidly vaporizing to form a gas-liquid two-phase flow. For example, the vacuum flash evaporator is equipped with a pressure reducing valve for adjusting the pressure reduction opening. The internal pressure of the vacuum flash evaporator can be controlled by adjusting the opening of the pressure reducing valve. In this application, the flash temperature is 60°C, and the temperature can be maintained directly using the residual heat of fermentation, avoiding acetone condensation. The concentration of gaseous acetone can be controlled by adjusting the opening of the pressure reducing valve, reaching 80–90% v / v.

[0029] The gas condenser 400 is used to condense the volatile acetone gas for easy collection. The gas condenser 400 has an inlet, a condensate outlet, and a gas outlet. The inlet of the gas condenser 400 is connected to the vapor phase outlet of the vacuum flash tank 300.

[0030] The acetone storage tank 500 is used to collect acetone, and the condensate outlet of the gas condenser 400 is connected to the acetone storage tank 500. The acetone storage tank 500 collects the condensed acetone to facilitate further purification, such as distillation.

[0031] The adsorption tower 600 has corresponding inlet and outlet ports. The tower is filled with adsorption particles for adsorbing acetone. The inlet of the adsorption tower is connected to the gas outlet of the gas condenser. In other words, acetone that has not been condensed by the gas condenser can be further adsorbed and recovered by the adsorption tower. For example, the adsorption tower can be an activated carbon adsorption tower filled with activated carbon, or a two-stage activated carbon adsorption tower. In this application, for trace amounts of uncondensed acetone (<100ppm), a two-stage activated carbon adsorption tower is used, achieving an adsorption efficiency ≥99.5%. After adsorption saturation, acetone is recovered by steam desorption (120-150℃), and the desorbed gas is returned to the primary condenser for re-liquefaction. For example, the adsorption tower has a recovery port connected to the inlet of the gas condenser. Alternatively, valves can be installed on the recovery port and the inlet of the gas condenser. It should be noted that valves can be installed on each connecting passage as needed in this application; further details on valves are not provided here. For example, when the adsorption tower uses steam desorption, the temperature is controlled at 120-150℃ and the operating pressure is atmospheric pressure. Activated carbon can be regenerated by steam, thus facilitating recycling.

[0032] The aforementioned acetone extraction apparatus for syngas pressure fermentation addresses the challenge of difficult gas-phase recovery caused by acetone boiling points exceeding 130°C during pressurized fermentation processes (e.g., 0.7 MPa). Firstly, a membrane filtration unit retains the fermentation broth cells, preserving their activity with minimal impact. Then, a vacuum flash evaporator depressurizes the fermentation broth before flash evaporation, utilizing residual heat to maintain a temperature of 60°C, enabling rapid acetone vaporization and forming a gas-liquid two-phase flow. This design not only improves acetone vaporization efficiency but also reduces additional cooling requirements and energy consumption. A condenser is then used to condense the acetone in the vapor, followed by adsorption to recover the uncondensed acetone, ensuring an acetone recovery rate of over 99.5% in the fermentation product. Compared to traditional distillation methods, this approach, through depressurization, condensation, and adsorption, offers relatively lower energy consumption, lower costs, and easier recovery.

[0033] In one embodiment, the liquid phase outlet of the vacuum flash evaporator 300 is connected to the syngas pressurized fermenter 100. For example, the product extraction device further includes a circulation pump and a pressurization module 700. The liquid phase outlet of the vacuum flash evaporator 300 is connected to the syngas pressurized fermenter 100 via the circulation pump and pressurization module 700. The circulation pump and pressurization module 700 are used to pressurize the refluxed fermentation broth, for example, to 0.7 MPa, to ensure that the pressure requirements of the syngas pressurized fermenter are met. The acetone-free fermentation broth (containing residual substrate and metabolic byproducts) at the bottom of the flash evaporator is pressurized to 0.7 MPa by a high-pressure pump and then returned to the fermenter to maintain system pressure balance.

[0034] In one embodiment, the gas condenser is a stepped-temperature gas condenser. This further reduces energy consumption. For example, the gas condenser includes a primary condenser and a secondary condenser connected in sequence. The temperature of the cooling medium in the primary condenser is higher than that in the secondary condenser. The condensate outlets of both the primary and secondary condensers are connected to the acetone storage tank. For example, the primary condenser cools the acetone vapor to 0–5°C, allowing for preliminary condensation of over 90% of the acetone vapor, resulting in liquid acetone with a purity ≥95%. For example, the secondary condenser cools the acetone vapor to -20°C to recover any remaining acetone. The acetone concentration in the exhaust gas after passing through the secondary condenser is ≤100 ppm. Then, an activated carbon adsorption tower is used to adsorb and recover acetone less than 100 ppm. The activated carbon adsorption tower adsorbs trace amounts of uncondensed acetone (<100 ppm). After adsorption saturation, acetone is recovered by steam desorption (120–150℃). The desorbed gas is returned to the primary condenser. The energy consumption for adsorbent regeneration can be provided by the waste heat from fermentation.

[0035] In one embodiment, the product extraction device further includes a short-path distillation column connected to the acetone storage tank. The short-path distillation column is used to distill and purify the crude acetone in the acetone storage tank. After passing through the short-path distillation column, the crude acetone can be used under vacuum conditions (operating temperature 40-50°C) to remove trace amounts of moisture and volatile impurities, increasing the acetone purity to 99.9%. In one embodiment, the shell of the short-path distillation column is made of 316L stainless steel, ensuring good safety. Furthermore, the temperature of the short-path distillation column is controlled at 40-50°C, and the operating pressure is controlled at 10-20 kPa.

[0036] The aforementioned acetone extraction apparatus for syngas pressure fermentation addresses the challenge of difficult gas-phase recovery caused by acetone boiling points exceeding 130°C during pressurized fermentation processes (e.g., 0.7 MPa). Firstly, a membrane filtration unit retains the fermentation broth cells, preserving their activity with minimal impact. Then, a vacuum flash evaporator depressurizes the fermentation broth before flash evaporation, utilizing residual heat to maintain a temperature of 60°C, enabling rapid acetone vaporization and forming a gas-liquid two-phase flow. This design not only improves acetone vaporization efficiency but also reduces additional cooling requirements and energy consumption. A condenser is then used to condense the acetone in the vapor, followed by adsorption to recover the uncondensed acetone, ensuring an acetone recovery rate of over 99.5% in the fermentation product. Compared to traditional distillation methods, this approach, through depressurization, condensation, and adsorption, offers relatively lower energy consumption, lower costs, and easier recovery. In other preferred embodiments, energy costs can be further reduced by using stepped temperature condensation through a primary condenser and a secondary condenser.

[0037] In this application, the product extraction device for acetone production via syngas pressure fermentation achieves efficient recycling of the fermentation broth and continuous acetone production through ceramic membrane retention of the bacterial cells, vacuum flash vaporization of acetone, and combined condensation-adsorption recovery. This application has the following technical advantages:

[0038] 1. High efficiency of cell retention and liquid-phase circulation

[0039] The ceramic membrane filtration unit can efficiently retain bacteria under high temperature and high pressure (60℃, 0.7MPa) conditions, with a bacterial retention rate of ≥99%, while maintaining a high membrane flux (50–100L / (m²)). 2 This not only prevents cell loss but also maintains the stability and efficiency of the fermentation system through liquid-phase circulation.

[0040] 2. Innovation of vacuum flash evaporation and acetone vaporization

[0041] By using vacuum flash evaporation technology, the fermentation broth is reduced from 0.7 MPa to atmospheric pressure (0.1 MPa), and the residual heat from fermentation is used to maintain the temperature (60°C), allowing acetone to rapidly vaporize and form a gas-liquid two-phase flow. This design not only improves the vaporization efficiency of acetone but also reduces the need for additional cooling, thus lowering energy consumption.

[0042] 3. High-efficiency recovery through multi-stage condensation and adsorption

[0043] A multi-stage gradient condensation system (first-stage condensation at 0–5℃, second-stage cryogenic condensation at -20℃) can efficiently recover acetone. The first-stage condensation alone can recover over 90% of the acetone vapor, with liquid acetone purity ≥95%. An activated carbon adsorption tower further treats trace amounts of acetone (<100ppm) in the exhaust gas, and adsorbent regeneration is achieved through steam desorption, resulting in an acetone concentration ≤100ppm in the exhaust gas. This multi-stage recovery design significantly improves the acetone recovery rate while reducing the acetone content in exhaust gas emissions, offering both environmental and economic benefits.

[0044] 4. System stability under pressurized liquid-phase reflux

[0045] The acetone-free fermentation broth at the bottom of the flash evaporator is pressurized to 0.7 MPa by a high-pressure pump and then returned to the fermenter to maintain system pressure balance. This design ensures the stability of the fermentation system while avoiding substrate waste and improving resource utilization.

[0046] 5. Closed-loop design and energy efficiency optimization of the overall system

[0047] This system achieves efficient recycling of fermentation broth and continuous acetone production through ceramic membrane retention of bacterial cells, vacuum flash vaporization of acetone, and combined condensation-adsorption recovery. Furthermore, the system integrates an energy recovery module, utilizing waste heat from fermentation to regenerate the adsorbent, further reducing energy consumption.

[0048] The aforementioned acetone extraction unit, developed through syngas pressure fermentation, innovatively integrates ceramic membrane filtration, vacuum flash evaporation, multi-stage condensation adsorption, and liquid-phase pressurized reflux modules, forming a highly efficient closed-loop online separation and circulation system. This design not only improves fermentation efficiency and acetone recovery rate but also significantly reduces energy consumption and exhaust emissions, resulting in substantial economic and environmental benefits.

[0049] The technical features of the embodiments described above can be combined arbitrarily. For the sake of brevity, not all possible combinations of the technical features in the above embodiments are described. However, as long as the combination of these technical features does not contradict each other, it should be considered within the scope of this specification. It should be noted that the terms "in one embodiment," "for example," and "as in another example" in this application are intended to illustrate the application and are not intended to limit the application.

[0050] The embodiments described above are merely illustrative of several implementations of this utility model, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the utility model patent. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of this utility model, and these all fall within the protection scope of this utility model. Therefore, the protection scope of this utility model patent should be determined by the appended claims.

Claims

1. A product extraction apparatus for the production of acetone by the pressure fermentation of synthesis gas, characterised in that, include: A syngas pressurized fermenter, wherein the syngas pressurized fermenter is used to produce acetone based on syngas fermentation, and the syngas pressurized fermenter has a fermentation broth outlet; A membrane filtration unit is provided with a filter membrane for retaining bacterial cells. The membrane filtration unit has an inlet, an outlet, and a reflux port. The inlet of the membrane filtration unit is connected to the fermentation broth outlet, and the reflux port of the membrane filtration unit is connected to the fermentation tank. A vacuum flash evaporator has a liquid inlet, a vapor phase outlet, and a liquid phase outlet, and the liquid inlet of the vacuum flash evaporator is connected to the liquid outlet of the membrane filtration unit. A gas condenser has an inlet, a condensate outlet, and a gas outlet, and the inlet of the gas condenser is connected to the vapor phase outlet of the vacuum flash tank. An acetone storage tank, wherein the condensate outlet of the gas condenser is connected to the acetone storage tank.

2. The product extraction device of claim 1, wherein, The liquid phase outlet of the vacuum flash evaporator is connected to the syngas pressurized fermenter; And / or, the product extraction device further includes an adsorption tower having opposing inlets and outlets, the adsorption tower being filled with adsorption particles for adsorbing acetone, and the inlet of the adsorption tower being connected to the gas outlet of the gas condenser.

3. The product extraction device of claim 2, wherein, The product extraction device also includes a circulation pump and a pressurization module. The liquid phase outlet of the vacuum flash tank is connected to the syngas pressurized fermenter through the circulation pump and the pressurization module.

4. The product extraction device of claim 1, wherein, The membrane filtration unit is a ceramic membrane filtration unit, which is equipped with a ceramic filter membrane that traps bacteria.

5. The product extraction device of claim 4, wherein, The ceramic filter membrane has a pore size of 0.1–0.2 μm.

6. The product extraction device of claim 1, wherein, The gas condenser is a stepped-temperature gas condenser.

7. The product extraction device of claim 6, wherein, The gas condenser includes a primary condenser and a secondary condenser connected in sequence. The temperature of the cooling medium in the primary condenser is higher than that in the secondary condenser. The condensate outlets of the primary condenser and the secondary condenser are both connected to the acetone storage tank.

8. The product extraction device of claim 2, wherein, The adsorption tower is an activated carbon adsorption tower, and the activated carbon adsorption tower is filled with activated carbon.

9. The product extraction device of claim 1, wherein, The pressure-reducing flash tank is equipped with a pressure-reducing valve for adjusting the pressure reduction opening.

10. The product extraction device of claim 1, wherein, The product extraction device also includes a short-path distillation column, which is connected to the acetone storage tank. The short-path distillation column is used to distill and purify the crude acetone in the acetone storage tank.

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