Waste treatment system and method for converting waste to energy

Abstract

To provide a method and a system for converting waste to energy with low environmental pollution and power consumption.SOLUTION: A method includes the steps of: (a) preparing a base containing fats and oils and reacting it with a biocatalyst to generate a surfactant molecular liquid; (b) pretreating organic waste with the surfactant molecular liquid to generate a first organic liquid; (c) performing sonication of the first organic liquid to generate a second organic liquid; and (d) performing anaerobic biological treatment of the second organic liquid to convert it to methane. The biocatalyst has at least one lipase. The surfactant molecular liquid has at least one of monoglyceride and diglyceride. A waste treatment system for converting waste to energy is also provided.SELECTED DRAWING: Figure 3

Description

[Technical Field]

[0001] FIELD OF THE DISCLOSURE The present disclosure relates to waste treatment systems and methods for converting waste to energy. [Background technology]

[0002] Current manufacturing contributes a significant amount of output to the global economy, but also generates large amounts of waste. As the circular economy becomes mainstream, industry and governments are placing greater emphasis on how to turn waste into resources and reduce carbon emissions.

[0003] While the goal of environmental protection is a sustainable environment, sludge from manufacturing industries, which contains a large amount of organic waste, is considered a recyclable resource, and how to effectively treat and utilize waste sludge is currently a key issue in the manufacturing industry. Among the current sludge treatment technologies, ultrasonic-based physical pretreatment methods are excellent in terms of reducing environmental pollution, but power consumption remains a major issue. Summary of the Invention [Problem to be solved by the invention]

[0004] As mentioned above, although existing waste sludge treatment technologies have largely met their intended uses, they do not completely satisfy all requirements in various aspects. Therefore, the development of an energy-saving waste sludge treatment method that shortens the treatment time or improves the treatment efficiency while maintaining the efficiency of ultrasonic treatment is a challenge that is being paid close attention to in related fields. [Means for solving the problem]

[0005] Some embodiments of the present disclosure provide a method for converting waste to energy, including the steps of: (a) providing an oil-containing base and reacting it with a biocatalyst to produce a surfactant molecule liquid; (b) pretreating organic waste with the surfactant molecule liquid to produce a first organic liquid; (c) sonicating the first organic liquid to produce a second organic liquid; and (d) subjecting the second organic liquid to anaerobic biological treatment to convert it to methane. The biocatalyst includes at least one lipase, and the reaction between the biocatalyst and the oil-containing base is carried out. weight ratio is 0.005 to 0.02:1, and the surfactant molecule liquid includes at least one of a monoglyceride and a diglyceride. 。

[0006] Some embodiments of the present disclosure also provide a waste treatment system including a surfactant molecule liquid generator, an ultrasonic generator, and an anaerobic bioreactor. The surfactant molecule liquid generator includes a biocatalyst, and the biocatalyst is used to treat an oil-containing base to produce surfactant molecule liquid. The ultrasonic generator is connected to the surfactant molecule liquid generator and is used to treat an organic liquid produced by mixing organic waste and the surfactant molecule liquid. The anaerobic bioreactor is connected to the ultrasonic generator and is used to treat the organic liquid to produce methane. The biocatalyst includes at least one lipase, and the biocatalyst and the oil-containing base are used to treat the organic liquid. weight ratio is 0.005 to 0.02:1, and the surfactant molecule liquid comprises at least one of a monoglyceride and a diglyceride.

[0007] Detailed description will be given in the following embodiments with reference to the accompanying drawings. [Brief explanation of the drawings]

[0008] The present invention can be more fully understood from the following detailed description and examples, taken in conjunction with the accompanying drawings. [Figure 1] 1 shows an illustration of a waste treatment system according to some embodiments of the present disclosure. [Figure 2] FIG. 1 shows a diagram illustrating how lipase (EC 3.1.1.3) catalyzes triglyceride hydrolysis reactions. [Figure 3] FIG. 1 illustrates a step flow diagram of a waste-to-energy method according to some embodiments of the present disclosure. [Figure 4] 1 shows the results of fat and oil conversion tests using lipases derived from various strains and biocatalysts with various compositional blend ratios according to some embodiments of the present disclosure. BSL represents a group of lipases derived from Bacillus subtilis, YLL represents a group of lipases derived from Yarrowia lipolytica, and ANL represents a group of lipases derived from Aspergillus niger. niger), BSL+YLL+ANL (1:1:1) is a group of lipases derived from Bacillus subtilis, Yarrowia lipolytica, and Aspergillus niger, and the weight ratio used for the lipases derived from Bacillus subtilis, Yarrowia lipolytica, and Aspergillus niger, respectively, is 1:1:1, and BSL+YLL+ANL (1:2:3) is a group of lipases derived from Bacillus subtilis, Yarrowia lipolytica, and Aspergillus niger, and the weight ratio used for the lipases derived from Bacillus subtilis, Yarrowia lipolytica, and Aspergillus niger, respectively, is 1:2:3. [Figure 5] 1 shows analytical results testing the effect of adding surfactant molecule liquid on the ultrasonic treatment of organic waste, according to some embodiments of the present disclosure. [Figure 6] 1 shows analytical results testing the effect of adding surfactant molecule liquid on the ultrasonic treatment of organic waste, according to some embodiments of the present disclosure. [Figure 7] 1 shows analytical results testing the effect of adding surfactant molecule liquid on anaerobic biological treatment (methane production potential) of organic waste, according to some embodiments of the present disclosure. DETAILED DESCRIPTION OF THE INVENTION

[0009] In the following description, the waste treatment system and method for converting waste to energy of the present disclosure will be described in detail. It should be understood that in the following detailed description, for purposes of explanation, numerous specific details and embodiments are set forth in order to provide a more complete understanding of the present disclosure. The specific elements and configurations described in the following detailed description are set forth for clarity of the present disclosure. It should be apparent that the exemplary embodiments shown herein are used for illustrative purposes only and are not intended to limit the present disclosure.

[0010] The description of the exemplary embodiments is intended to be read in connection with the accompanying drawings, which are to be considered part of the entire description. It should be understood that the figures are not drawn to scale. In fact, the sizes of elements may be arbitrarily increased or decreased to clearly depict the features of the present disclosure.

[0011] 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 disclosure belongs. In various cases, it should be understood that terms defined in commonly used dictionaries should be interpreted to have a meaning consistent with the relevant art of this disclosure and the background or context of this disclosure, and should not be interpreted in an idealized or overly formal manner unless so defined.

[0012] In response to the current industrial need for reducing waste sludge and the market need for related technology products and services, embodiments of the present disclosure provide a method for converting waste to energy that uses biocatalytic technology together with ultrasonic sludge treatment technology and a resource-to-energy unit to produce biomass methane, thereby establishing a waste treatment system with high treatment efficiency and energy savings. According to embodiments of the present disclosure, the waste-to-energy method and waste treatment system can increase the rate at which organic waste is converted into biomass methane for reuse, reduce the cost of organic waste treatment, and increase the production of biomass green electricity, while simultaneously achieving carbon reduction through waste reduction and energy conversion of waste resources.

[0013] 1 shows an illustration of a waste treatment system 10 according to some embodiments of the present disclosure. It should be understood that for clarity, the drawing omits some components of the waste treatment system 10 and shows only some components illustratively. According to one embodiment, additional features may be added to the waste treatment system 10, as described below.

[0014] See Figure 1. The waste treatment system 10 may include a surfactant molecule liquid generator 110, an ultrasonic generator 120, and an anaerobic biological reactor 130. The ultrasonic generator 120 may be connected to the surfactant molecule liquid generator 110, and the anaerobic biological reactor 130 may be connected to the ultrasonic generator 120. The ultrasonic generator 120 may be located downstream of the surfactant molecule liquid generator 110, and the anaerobic biological reactor 130 may be located downstream of the ultrasonic generator 120. According to some embodiments, the surfactant molecule liquid generator 110, the ultrasonic generator 120, and the anaerobic biological reactor 130 may be connected via piping.

[0015] The surfactant molecule liquid generator 110 may include a biocatalyst 110c, which can be used to process the oil-containing base W1 to produce the surfactant molecule liquid SC. According to some embodiments, the oil-containing base W1 may be supplied by a substrate supply unit (not shown), which may be connected to the surfactant molecule liquid generator 110.

[0016] According to some embodiments, the fat-and-oil-containing base W1 may include, but is not limited to, a medium- and long-chain triglyceride (MLCT) having a carbon number of C12-C20, such as, for example, a triglyceride having a carbon number of C12, C14, C16, C18, or C20. According to some embodiments, the fat-and-oil-containing base W1 may include, but is not limited to, a long-chain triglyceride having a carbon number of C16-C20. According to some embodiments, the fat-and-oil-containing base W1 may include, but is not limited to, food industry wastewater, manufacturing wastewater, edible oil, feed oil, recycled oils of the aforementioned oils, other suitable oils, or combinations of the aforementioned.

[0017] Biocatalyst 110c may include at least one lipase. Additionally, the lipase may be immobilized on a support, and the support matrix may include, but is not limited to, chitosan or other suitable support matrix. According to some embodiments, the lipase may include, but is not limited to, triglyceride lipase (EC 3.1.1.3). According to some embodiments, the lipase may be derived from at least one of Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis. According to some embodiments, the lipase may be derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis, and the lipase may be derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis, respectively. weight ratiomay be 1-3:1-3:1-3. Lipases derived from multiple strains can particularly provide a preferred broad spectrum and can improve the efficiency of the lipase in catalyzing the hydrolysis of fats and oils.

[0018] The surfactant liquid SC produced by the action of lipase on the fat-and-oil-containing base W1 is a liquid with surface-active properties, and may contain at least one of monoglycerides and diglycerides. For example, see FIG. 2. FIG. 2 shows an explanatory diagram illustrating how lipase (EC 3.1.1.3) catalyzes the hydrolysis of triglycerides. Lipase acts on the ester bonds of fat and oil molecules, hydrolyzing triglycerides into diglycerides and fatty acids, which can then be hydrolyzed into monoglycerides and fatty acids, and then the monoglycerides into glycerin and fatty acids. It should be noted that the monoglycerides and diglycerides in the surfactant liquid SC have emulsifier-like properties, which, when subsequently reacting with organic waste W2, can increase the solubility and homogeneity of the organic waste W2, reduce the surface tension of the mixed liquid to be treated, and shorten the time required for subsequent ultrasonic treatment. Additionally, the liberated fatty acid molecules can serve as precursor nutrients that anaerobic organisms can convert to methane, increasing biomass methane production in the subsequent processing step in the anaerobic reactor 130.

[0019] Furthermore, the biocatalyst and the oil-containing base W1 weight ratioThe ratio may be 0.005 to 0.02:1, for example, 0.006:1, 0.007:1, 0.008:1, 0.009:1, 0.01:1, 0.011:1, 0.012:1, 0.013:1, 0.014:1, 0.015:1, 0.016:1, 0.017:1, 0.018:1, or 0.019:1, but is not limited thereto. In particular, if the ratio of biocatalyst to oil-containing base W1 is too low (e.g., lower than 0.005:1), the time required for lipase action may be excessively long, potentially reducing the processing efficiency of the surfactant molecule liquid generator 110. On the other hand, if the ratio of biocatalyst to oil-containing base W1 is too high (e.g., higher than 0.02:1), production costs may increase significantly.

[0020] According to some embodiments, surfactant molecule liquid SC can be produced by reacting the oil-containing base W1 with the biocatalyst 110c in the surfactant molecule liquid generator 110 at a temperature of 25°C to 45°C and a pH of 6.5 to 7.5. According to some embodiments, the reaction temperature of the surfactant molecule liquid generator 110 is 25°C to 40°C or 25°C to 35°C, such as, but not limited to, 26°C, 27°C, 28°C, 29°C, 30°C, 31°C, 32°C, 33°C, or 34°C. According to some embodiments, the reaction pH of the surfactant molecule liquid generator 110 can be, but is not limited to, 6.6, 6.7, 6.8, 6.9, 7, 7.1, 7.2, 7.3, or 7.4.

[0021] Furthermore, according to some embodiments, the waste treatment system 10 may further include a surfactant molecule liquid storage tank 112, which is connected to the surfactant molecule liquid generator 110 and can be used to temporarily store the surfactant molecule liquid SC, and which may further be connected to an ultrasonic generator 120 so that the surfactant molecule liquid SC can be sent to the ultrasonic generator 120.

[0022] Specifically, the surfactant molecule liquid SC can be mixed with the organic waste W2 before being sent to the ultrasonic generator 120. By pretreating the organic waste W2 with the surfactant molecule liquid SC, a first organic liquid OG can be produced, and the treated first organic liquid OG can be decomposed into a homogeneous organic liquid having relatively small molecules, such as organic sludge.

[0023] According to some embodiments, the organic waste W2 may be supplied by a waste supply unit (not shown), which may be connected to the ultrasonic generator 120. Specifically, the piping of the waste supply unit is connected to the piping of the surfactant molecule liquid generator 110, and then both are connected to the ultrasonic generator 120.

[0024] According to some embodiments, the organic waste W2 may include, but is not limited to, manufacturing waste, petrochemical waste, agricultural waste, livestock waste, food waste, other suitable organic waste, or combinations of the foregoing.

[0025] As described above, the surfactant molecule liquid SC produced after the oil-containing base W1 is processed in the surfactant molecule liquid generator 110 contains at least one of monoglycerides and diglycerides. Monoglycerides and diglycerides have emulsifier-like functions, which can increase the solubility and homogeneity of the organic waste W2, reduce the surface tension of the mixed liquid to be processed, and shorten the time required for the subsequent ultrasonic treatment.

[0026] According to some embodiments, a mixture of surfactant molecule liquid SC and organic waste W2 in a homogeneous first organic liquid OG is Volume ratio may be 0.005 to 0.05:1, for example, but not limited to, 0.01:1, 0.015:1, 0.02:1, 0.025:1, 0.03:1, 0.035:1, 0.04:1, or 0.045:1. It should be noted that when the ratio of the surfactant molecule liquid SC to the organic waste W2 is within the above-mentioned range, the treatment efficiency of the surfactant molecule liquid SC with respect to the organic waste W2 can be effectively increased.

[0027] According to some embodiments, the pretreatment of the organic waste W2 with the surfactant liquid SC involves a continuous reaction at a temperature of 20° C. to 60° C. and a pH of 5 to 8. According to some embodiments, the reaction temperature of the pretreatment may be 30° C. to 50° C. or 30° C. to 40° C., such as, but not limited to, 22° C., 24° C., 26° C., 27° C., 28° C., 29° C., 30° C., 31° C., 32° C., 33° C., 34° C., 35° C., 36° C., 37° C., 38° C., 39° C., 42° C., 45° C., 48° C., 52° C., 55° C., or 58° C. According to some embodiments, the reaction pH of the pretreatment may be 6.5 to 7.5, such as, but not limited to, 6.6, 6.7, 6.8, 6.9, 7, 7.1, 7.2, 7.3, or 7.4.

[0028] The ultrasonic generator 120 is also used to treat the first organic liquid OG, which is produced by mixing the organic waste W2 with the surfactant molecule liquid SC, to produce a second organic liquid OG'. The ultrasonic generator 120 applies ultrasonic energy to the first organic liquid OG to hydrolyze the organic matter and improve the efficiency of the subsequent biological anaerobic treatment performed in the anaerobic biological reactor 130. Specifically, the impact force generated by the cavitation effect provided by the ultrasonic waves destroys the structure of the first organic liquid OG (e.g., the cell walls of microorganisms in organic sludge), thereby increasing the concentration of dissolved organic matter in the first organic liquid OG, making it easier for subsequent anaerobic microorganisms to digest it, and ultimately reducing the time required for the biological anaerobic treatment plant.

[0029] According to some embodiments, the output power of the sonication may be from 300 Watts to 1200 Watts, such as, but not limited to, 400 Watts, 500 Watts, 600 Watts, 700 Watts, 800 Watts, 900 Watts, 1000 Watts, or 1100 Watts. According to some embodiments, the frequency of the sonication may be from 20 kilohertz (kHz) to 100 kHz, such as, but not limited to, 30 kHz, 40 kHz, 50 kHz, 60 kHz, 70 kHz, 80 kHz, or 90 kHz.

[0030] The anaerobic biological reactor 130 can be used to treat the second organic liquid OG' to produce methane MT, which can be provided to a downstream swamp gas power plant for conversion into electrical energy. Specifically, anaerobic biological treatment can decompose and convert small organic molecules through microbial biochemical metabolism to produce swamp gases, such as methane. According to some embodiments, the anaerobic biological reactor 130 can include, but is not limited to, hydrolytic bacteria, acid-forming bacteria, methanogens, other suitable bacterial species, or a combination of the foregoing.

[0031] According to some embodiments, the anaerobic biological treatment in the anaerobic biological reactor 130 proceeds at a temperature of 25° C. to 45° C. and a pH of 6.8 to 7.2. According to some embodiments, the reaction temperature of the anaerobic biological treatment may be 30° C. to 40° C., such as, but not limited to, 26° C., 27° C., 28° C., 29° C., 30° C., 31° C., 32° C., 33° C., 34° C., 35° C., 36° C., 37° C., 38° C., 39° C., 40° C., 41° C., 42° C., 43° C., or 44° C. According to some embodiments, the reaction pH of the anaerobic biological treatment may be, but is not limited to, pH 6.9, pH 7, or pH 7.1.

[0032] The present disclosure also provides a method 20 for converting waste to energy. Figure 3 illustrates a step flow diagram of the method 20 for converting waste to energy, according to some embodiments of the present disclosure. According to some embodiments, the method 20 for converting waste to energy includes treating organic waste using the waste treatment system 10 described above, although the present disclosure is not limited thereto. It should be understood that, according to some embodiments, additional steps can be added, or steps can be substituted or omitted, before, during, and / or after the method 20 for converting waste to energy described below.

[0033] As shown in FIG. 3, the method 20 for converting waste to energy may include step S1 of providing an oil-containing base W1 and reacting it with a biocatalyst 110c to produce a surfactant molecule liquid SC.

[0034] According to some embodiments, the fat-and-oil base W1 may include a medium- or long-chain triglyceride having a carbon number of C12-C20, such as, but not limited to, a triglyceride having a carbon number of C12, C14, C16, C18, or C20. According to some embodiments, the fat-and-oil base W1 may include a long-chain triglyceride having a carbon number of C16-C20. According to some embodiments, the fat-and-oil base W1 may include, but is not limited to, food industry wastewater, manufacturing wastewater, edible oil, feed oil, recycled oils of the aforementioned oils, other suitable oils, or combinations of the aforementioned.

[0035] Biocatalyst 110c may include at least one lipase. Additionally, the lipase may be immobilized on a support, which may include, but is not limited to, chitosan or other suitable support materials. According to some embodiments, the lipase may include, but is not limited to, a triglyceride lipase (EC 3.1.1.3). According to some embodiments, the lipase may be derived from at least one of Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis. According to some embodiments, the lipase may be derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis, and the lipases derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis may be used. weight ratio The ratio may be 1-3:1-3:1-3, for example, 1:1:1, 1:1:2, 1:1.5:2, 1:1.8:2.5, 1:2:3, 1:2.5:3, 1:3:2, 1:3:1.5, 2:1:2, 2:1:2.5, 2:1:3, 2:2:1, 2:2.5:1.8, 2:3:1, 3:1:2, 3:1.8:1.5, 3:2:1, 3:2.5:1, 3:3:1, or 3:3:2. Lipases derived from multiple strains can provide a broader spectrum of activity and improve the efficiency of lipases in catalyzing the hydrolysis of fats and oils. Furthermore, lipases derived from the aforementioned specific strains have good substrate compatibility and exhibit excellent catalytic performance, especially for medium- and long-chain triglycerides with carbon numbers of C12-C20.

[0036] The surfactant molecule liquid SC produced by subjecting the fat-and-oil-containing base W1 to the action of lipase may contain at least one of monoglycerides and diglycerides. The monoglycerides and diglycerides in the surfactant molecule liquid SC have emulsifier-like properties, which, when subsequently reacted with the organic waste W2, can increase the solubility and homogeneity of the organic waste W2, reduce the surface tension of the treated mixture, and shorten the time required for subsequent ultrasonic treatment. Furthermore, the liberated fatty acid molecules can serve as precursor nutrients for anaerobic organisms to convert to methane, thereby increasing biomass methane production.

[0037] Furthermore, the biocatalyst and the oil-containing base W1 weight ratio The ratio of the biocatalyst to the fat-and-oil-containing base W1 may be, but is not limited to, 0.005 to 0.02:1, for example, 0.006:1, 0.007:1, 0.008:1, 0.009:1, 0.01:1, 0.011:1, 0.012:1, 0.013:1, 0.014:1, 0.015:1, 0.016:1, 0.017:1, 0.018:1, or 0.019:1. In particular, if the ratio of the biocatalyst to the fat-and-oil-containing base W1 is too low (e.g., lower than 0.005:1), the time required for the lipase action may be excessively long, potentially reducing the processing efficiency. On the other hand, if the ratio of the biocatalyst to the fat-and-oil-containing base W1 is too high (e.g., higher than 0.02:1), production costs may increase significantly.

[0038] According to some embodiments, step S1 is carried out at a temperature of 25° C. to 45° C. and a pH of 6.5 to 7.5 for 1 to 9 hours. According to some embodiments, the reaction temperature in step S1 may be 25° C. to 40° C. or 25° C. to 35° C., such as, but not limited to, 26° C., 27° C., 28° C., 29° C., 30° C., 31° C., 32° C., 33° C., 34° C., 35° C., 36° C., 37° C., 38° C., 39° C., 40° C., 41° C., 42° C., 43° C., or 44° C. According to some embodiments, the reaction pH in step S1 may be, but is not limited to, pH 6.6, pH 6.7, pH 6.8, pH 6.9, pH 7, pH 7.1, pH 7.2, pH 7.3, or pH 7.4. According to some embodiments, the reaction time of step S1 may be, but is not limited to, 1.5 hours, 2 hours, 2.5 hours, 3 hours, 3.5 hours, 4 hours, 4.5 hours, 5 hours, 5.5 hours, 6 hours, 6.5 hours, 7 hours, 7.5 hours, 8 hours, or 8.5 hours.

[0039] Also, according to some embodiments, step S1 further includes adjusting the fat content of the fat-containing base W1 to 30 wt% to 50 wt%, for example, but not limited to, 35 wt%, 40 wt%, or 45 wt%. It should be noted that if the fat content in the fat-containing base W1 is too high (for example, higher than 50 wt%), lipase may not be able to act effectively, which may result in poor fat hydrolysis.

[0040] Additionally, the waste-to-energy method 20 may include a step S2 of pre-treating organic waste W2 with a surfactant molecule liquid SC to produce a first organic liquid OG.

[0041] According to some embodiments, the organic waste W2 may include, but is not limited to, manufacturing waste, petrochemical waste, agricultural waste, livestock waste, food waste, other suitable organic waste, or combinations of the foregoing.

[0042] As mentioned above, the surfactant molecule liquid SC contains at least one of monoglyceride and diglyceride, and monoglyceride and diglyceride have emulsifier-like functions, which can increase the solubility and homogeneity of the organic waste W2, reduce the surface tension of the mixed liquid to be treated, and shorten the time required for the subsequent ultrasonic treatment.

[0043] According to some embodiments, in step S2, the surfactant molecule liquid SC and the organic waste W2 are mixed. Volume ratio may be 0.005 to 0.05:1, for example, but not limited to, 0.01:1, 0.015:1, 0.02:1, 0.025:1, 0.03:1, 0.035:1, 0.04:1, or 0.045:1. It should be noted that when the ratio of the surfactant molecule liquid SC to the organic waste W2 is within the above-mentioned range, the treatment efficiency of the surfactant molecule liquid SC with respect to the organic waste W2 can be effectively increased.

[0044] According to some embodiments, step S2 allows the continuous reaction to proceed under conditions of a temperature of 20° C. to 60° C. and a pH of 5 to 8. According to some embodiments, the reaction temperature in step S2 may be 30° C. to 50° C. or 30° C. to 40° C., for example, but not limited to, 22° C., 24° C., 26° C., 27° C., 28° C., 29° C., 30° C., 31° C., 32° C., 33° C., 34° C., 35° C., 36° C., 37° C., 38° C., 39° C., 42° C., 45° C., 48° C., 52° C., 55° C., or 58° C. According to some embodiments, the reaction pH in step S2 may be 6.5 to 7.5, for example, but not limited to, 6.6, 6.7, 6.8, 6.9, pH 7, pH 7.1, pH 7.2, pH 7.3, or pH 7.4.

[0045] Additionally, the waste-to-energy method 20 may include a step S3 of sonicating the first organic liquid OG to produce a second organic liquid OG'.

[0046] According to some embodiments, the output power of the sonication may be between 300 Watts and 1200 Watts, such as, but not limited to, 400 Watts, 500 Watts, 600 Watts, 700 Watts, 800 Watts, 900 Watts, 1000 Watts, or 1100 Watts. According to some embodiments, the frequency of the sonication may be between 20 kHz and 100 kHz, such as, but not limited to, 30 kHz, 40 kHz, 50 kHz, 60 kHz, 70 kHz, 80 kHz, or 90 kHz.

[0047] Additionally, the waste-to-energy method 20 may further include a step S4 of subjecting the second organic liquid OG' to anaerobic biological treatment to convert it into methane MT.

[0048] According to some embodiments, step S4 may include, but is not limited to, performing anaerobic bioremediation using hydrolytic bacteria, acidogenic bacteria, methanogenic bacteria, other suitable bacterial species, or a combination of the foregoing. According to some embodiments, step S4 is performed at a temperature of 25°C to 45°C and a pH of 6.8 to 7.2. According to some embodiments, the reaction temperature in step S4 may be 30°C to 40°C, such as, but not limited to, 26°C, 27°C, 28°C, 29°C, 30°C, 31°C, 32°C, 33°C, 34°C, 35°C, 36°C, 37°C, 38°C, 39°C, 40°C, 41°C, 42°C, 43°C, or 44°C. According to some embodiments, the reaction pH in step S4 may be, but is not limited to, pH 6.9, pH 7, or pH 7.1.

[0049] In order to make the above and other objects, features and advantages of the present disclosure more complete and easily understandable, numerous embodiments are presented below and described in detail as follows, but they are not intended to limit the scope of the present disclosure.

[0050] Example 1 - Preparation of biocatalyst

[0051] A 2% chitosan solution was prepared by dissolving chitosan in 1% acetic acid. The chitosan solution was then added dropwise to a 10% sodium hydroxide solution using a syringe. The chitosan gel beads were allowed to solidify in the solution and then left at room temperature for 60 minutes. After 60 minutes, the beads were washed repeatedly with deionized water until neutral. The 2% chitosan-containing gel beads were then crosslinked with a 0.25% glutaraldehyde solution and immobilized in a 500 U / g lipase solution (EC 3.1.1.3, derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis in a 1:1:1 ratio). After 180 minutes, the beads were removed and washed to produce chitosan gel beads containing immobilized lipase. The immobilized enzyme retained 72.6% of its enzyme activity compared with the free enzyme, and after 10 batches of fat and oil hydrolysis reactions, the retention rate reached 88.2%. This demonstrates that the biocatalysts prepared according to the examples of the present disclosure have good enzyme activity and stability and can be applied to waste treatment systems.

[0052] Example 2 - Preparation of surfactant molecular liquid

[0053] Food factory wastewater containing medium- and long-chain triglycerides was used as a fat-containing base, and its fat content was adjusted to the range of 30-50 wt%. The fat-containing base was used as a substrate raw material for preparing a surfactant molecular liquid. Next, the fat-containing base was reacted with the biocatalyst prepared in Example 1. weight ratio The conversion reaction was carried out as a batch process at a temperature of 25 to 45°C and a pH of 6.5 to 7.5 for 1 to 3 hours, producing a surfactant liquid containing monoglycerides, diglycerides, and free fatty acid molecules through catalytic action.

[0054] Example 3 - Oil and fat conversion test of biocatalysts with lipases of different strains and compositions

[0055] The same food factory wastewater as in Example 2 was used as the fat-containing base, which was diluted to a fat content of 50 wt%. The fat-containing base was used as the substrate for this reaction test. Furthermore, five groups of biocatalysts were prepared with the originating strains and compositions shown in Table 1 below.

[0056] [Table 1]

[0057] The test was divided into five groups. 100 g of the aforementioned oil-containing base was used as the substrate for the reaction test, and 2 g of each of the five biocatalysts with different compositions was added. The reaction proceeded with uniform stirring at 30°C and pH 7.0. After the reaction time reached 3, 6, and 9 hours, 1 ml of the reaction mixture was taken and analyzed for fat degradation rates to obtain data on the fat conversion rates of the five biocatalysts with different compositions. The results are shown in Figure 4. BSL represents group 1, which contains lipases derived from Bacillus subtilis; YLL represents group 2, which contains lipases derived from Yarrowia lipolytica; ANL represents group 3, which contains lipases derived from Aspergillus niger; and BSL+YLL+ANL (1:1:1) represents lipases derived from Bacillus subtilis, Yarrowia lipolytica, and Aspergillus niger ( weight ratio Group 4, derived from BSL+YLL+ANL (1:2:3), was a lipase-producing strain of Bacillus subtilis, Yarrowia lipolytica, and Aspergillus niger ( weight ratio Group 5 is derived from the 1:2:3) ancestry.

[0058] As shown in Figure 4, the oil conversion rates of the single-strain BSL after 3, 6, and 9 hours of reaction were 12%, 14%, and 15%, respectively. The oil conversion rates of the single-strain YLL after 3, 6, and 9 hours of reaction were 21%, 24%, and 26%, respectively. The oil conversion rates of the single-strain ANL after 3, 6, and 9 hours of reaction were 25%, 32%, and 37%, respectively. The oil conversion rates of the multi-strain BSL + YLL + ANL (1:1:1) after 3, 6, and 9 hours of reaction were 38%, 46%, and 50%, respectively. The oil conversion rates of the multi-strain BSL + YLL + ANL (1:2:3) after 3, 6, and 9 hours of reaction were 49%, 52%, and 53%, respectively.

[0059] As can be seen from the above results, both the single-strain and multi-strain lipase biocatalysts can catalyze oil conversion, but the multi-strain lipase biocatalyst has a better conversion catalytic effect, especially when the ratio of Aspergillus niger is high (BSL+YLL+ANL (1:2:3)).

[0060] Example 4 - Oil conversion rate test for various oils and fats used as substrate raw materials using biocatalysts

[0061] Two types of oils with different carbon chain lengths, olive oil (long-chain triglycerides (LCT)) and coconut oil (medium-chain triglycerides (MCT)), were used as substrates in this reaction test, and the same multi-strain BSL+YLL+ANL (1:1:1) biocatalysts as described in Example 3 were added to prepare surfactant molecular liquids. After the reaction, the conversion rates of these two types of oils with different chain lengths were analyzed.

[0062] The test was divided into two groups, and 100g of each of the water samples containing 50wt% olive oil and 50wt% coconut oil as mentioned above was taken as the substrate for this reaction test. 2g of the biocatalyst BSL+YLL+ANL (1:1:1) derived from the same multiple strains as described in Example 3 was added to each, and the reaction was carried out by uniform stirring at a temperature of 30°C and pH 7.0. After 3 hours, 1ml of the reaction liquid was taken and an analysis of the oil decomposition rate was performed to obtain data on the oil conversion rate when the two different oil types mentioned above were used as substrates.

[0063] The results showed that the oil conversion rate for the olive oil (LCT)-containing water sample was approximately 51%, and the oil conversion rate for the coconut oil (MCT)-containing water sample was approximately 23%. As can be seen from the above results, both long-carbon chain oils and medium-carbon chain oils can be substrates for biocatalysts derived from multiple strains.

[0064] Example 5 - Organic waste decomposition test

[0065] Solid sludge waste from the petrochemical industry was used as organic waste. This organic waste was mixed with the surfactant molecule liquid prepared in Example 2 to prepare a homogeneous organic liquid. After ultrasonic treatment, the chemical oxygen demand (COD) (i.e., the concentration of soluble organic matter, in mg / L) of the ultrasonically treated reaction hydrolyzate was measured, and the effectiveness of ultrasonic pretreatment was evaluated based on this data.

[0066] 250 ml of organic sludge was mixed with 250 ml of purified water and 250 ml of surfactant liquid, and measurements were performed. The suspended solids (SS) concentration in the organic sludge was 10,256 mg / L, and the volatile suspended solids (VSS) concentration was 7,423 mg / L. The sludge was then treated with ultrasound at a frequency of 20 kHz and an output of 500 watts for 2.5, 5, 7.5, and 10 minutes, respectively. The results are shown in Figure 5.

[0067] Figure 5 shows the results of soluble organic matter concentration analysis for experimental samples that had not undergone any pretreatment (organic sludge with added pure water but not ultrasonicated), had not received surfactant liquid (organic sludge with added pure water and ultrasonicated), and had received surfactant liquid (organic sludge with added surfactant liquid and ultrasonicated), after ultrasonic treatment for 2.5, 5, 7.5, and 10 minutes, respectively.

[0068] As shown in Figure 5, the sample that had not undergone any pretreatment maintained a dissolved organic matter concentration of 208 mg / L, and the dissolved organic matter concentrations of the sample without surfactant liquid added were 1755 mg / L, 2508 mg / L, 3106 mg / L, and 3512 mg / L, respectively, after 2.5, 5, 7.5, and 10 minutes of ultrasonic treatment. The dissolved organic matter concentrations of the sample with surfactant liquid added were 3226 mg / L, 3806 mg / L, 3921 mg / L, and 4008 mg / L, respectively, after 2.5, 5, 7.5, and 10 minutes of ultrasonic treatment.

[0069] The concentration of dissolved organic matter in the sample without surfactant liquid added after 10 minutes of ultrasonic treatment was 3512 mg / L, while the concentration of dissolved organic matter in the sample with surfactant liquid added after 10 minutes of ultrasonic treatment increased to 4008 mg / L, improving the decomposition efficiency of organic waste by approximately 14%.

[0070] Next, please refer to Figure 6, which is a line graph of the experimental results of Figure 5. As shown in Figure 6, the dissolved organic matter concentration after 5 minutes of ultrasonic treatment of the sample with surfactant liquid added reached 3806 mg / L (power consumption 42 W), which was already higher than the 3512 mg / L (power consumption 83 W) reached after 10 minutes of ultrasonic treatment of the sample without surfactant liquid added.

[0071] As can be seen from the above results, compared to the ultrasonic sludge treatment method that does not use a biocatalyst (no surfactant molecule liquid added), the treatment method that uses a biocatalyst (surfactant molecule liquid added) together with ultrasonic sludge treatment technology requires only half the power consumption (reduced from 83W to 42W), and increased the soluble organic matter concentration of the treated material to 3512mg / L, effectively increasing the treatment efficiency by more than 50%.

[0072] Example 6 - Methane production potential test

[0073] The experiment was divided into two groups, with three identical 600ml reaction bottles prepared for each group. Each reaction bottle contained 350ml of thoroughly mixed organic hydrolysis sludge substrate (prepared in Example 5, but with or without surfactant liquid) and 150ml of seed sludge (sludge removed from the anaerobic biological treatment tank of a food processing wastewater treatment plant, containing common anaerobic species such as hydrolytic bacteria, oxidizing bacteria, and methanogens) and was shaken and stirred for over 21 days at 35°C and pH 7.0. A gas collection hole was installed above the reaction bottle lid, and gas generated by the decomposition of the organic hydrolysis sludge was collected daily using the water displacement method. The cumulative gas generation for each test sample was recorded. The results are shown in Figure 7.

[0074] As shown in Figure 7, the reaction was nearly complete on the 11th day of anaerobic biological treatment, with the cumulative gas generation volume of the organic waste hydrolyzed sludge without surfactant liquid being 99 ml, and the cumulative gas generation volume of the organic waste hydrolyzed sludge with surfactant liquid being 121 ml. Based on this, it can be estimated that the amount of methane generated from the sample with surfactant liquid added increased by approximately 22% compared to the sample without surfactant liquid added, effectively increasing the effectiveness of converting waste into energy.

[0075] In summary, the waste-to-energy method provided by the present disclosure uses biocatalytic technology in conjunction with ultrasonic sludge treatment technology and a resource-to-energy unit to produce biomass methane, thereby establishing a waste treatment system with high treatment efficiency and energy conservation. The waste-to-energy method and waste treatment system according to the present disclosure can increase the rate at which organic waste is converted into biomass methane for reuse, reduce organic waste treatment costs, and increase the production of biomass green power, while simultaneously achieving carbon reduction through waste reduction and the conversion of waste resources into energy.

[0076] Although some embodiments of the present disclosure and their advantages have been described above, it should be understood that substitutions and modifications can be made thereto without departing from the spirit and scope of the present disclosure as defined by the appended claims. In addition, each claim constitutes an independent embodiment, and the scope of claims of the present disclosure also includes combinations of such claims and embodiments. The scope of protection of the present disclosure is defined by the appended claims. [Explanation of symbols]

[0077] 110...Surface active molecular liquid generator 110c...biocatalyst 112...Surface active molecule liquid storage tank 120...Ultrasonic generator 130...Anaerobic biological reactor W1: Oil-containing base W2: Organic waste OG...the first organic liquid OG'...Second organic liquid MT…methane SC…surfactant molecular liquid

Claims

1. 1. A method for converting waste to energy, comprising: (a) providing an oil-containing base and reacting it with a biocatalyst to produce a surfactant molecule liquid; (b) pretreating organic waste with the surfactant molecule liquid to produce a first organic liquid, wherein the organic waste comprises manufacturing waste, petrochemical waste, agricultural waste, livestock waste, food waste, or a combination thereof, and the volume ratio of the surfactant molecule liquid to the organic waste is 0.005-0.05:1; (c) sonicating the first organic liquid to form a second organic liquid; (d) subjecting the second organic liquid to anaerobic biological treatment to convert it to methane; Including, 1. A method for converting waste to energy, wherein the biocatalyst comprises at least one lipase, the weight ratio of the biocatalyst to the oil-containing base is 0.005 to 0.02:1, and the surfactant molecular liquid comprises at least one of a monoglyceride and a diglyceride.

2. 2. The method of converting waste to energy of claim 1, wherein the oil-containing base comprises food industry wastewater, manufacturing wastewater, edible oil, feed oil, recycled oil of the aforementioned oils, or a combination of the aforementioned.

3. 2. The method of converting waste to energy according to claim 1, wherein the fat-and-oil-containing base comprises C12-C20 medium- and long-chain triglycerides (MLCTs).

4. 10. The method of converting waste to energy of claim 1, wherein step (a) further comprises adjusting the fat content of the fat-containing base to between 30 wt% and 50 wt%.

5. 2. The method for converting waste into energy according to claim 1, wherein step (a) comprises reacting at a temperature of 25°C to 45°C and at a pH of 6.5 to 7.5 for 1 hour to 9 hours.

6. 2. The method for converting waste to energy according to claim 1, wherein the lipase comprises a triglyceride lipase (EC 3.1.1.3).

7. 7. The method of converting waste to energy according to claim 6, wherein the lipase is derived from at least one of Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis.

8. 8. The method for converting waste into energy according to claim 7, wherein the lipases are derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis, and the weight ratio of the lipases derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis, respectively, is 1-3:1-3:1-3.

9. 2. The method for converting waste to energy according to claim 1, wherein in step (c), the output power of the ultrasonic treatment is between 300 watts and 1200 watts, and the frequency is between 20 kHz and 100 kHz.

10. a surfactant molecule liquid generator including a biocatalyst used to process an oil-containing base to produce a surfactant molecule liquid; an ultrasonic generator connected to the surfactant molecule liquid generator, for treating the organic liquid produced by mixing the organic waste and the surfactant molecule liquid; an anaerobic biological reactor connected to the ultrasonic generator and used to treat the organic liquid to produce methane; A waste treatment system comprising: the organic waste includes manufacturing waste, petrochemical waste, agricultural waste, livestock waste, food waste, or a combination thereof, and the volume ratio of the surfactant molecule liquid to the organic waste is 0.005-0.05:1; The waste treatment system, wherein the biocatalyst comprises at least one lipase, the weight ratio of the biocatalyst to the oil-containing base is 0.005 to 0.02:1, and the surfactant molecular liquid comprises at least one of a monoglyceride and a diglyceride.

11. 11. The waste treatment system according to claim 10, wherein the oil-containing base comprises a triglyceride having carbon atoms of C12 to C20, and the lipase comprises a triglyceride lipase (EC 3.1.1.3).

12. 12. The waste treatment system of claim 11, wherein the lipase is derived from at least one of Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis.

13. 13. The waste treatment system according to claim 12, wherein the lipases are derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis, and the weight percentages of the lipases derived from Aspergillus niger, Yarrowia lipolytica, and Bacillus subtilis, respectively, are 1-3:1-3:1-3.

14. 11. The waste treatment system according to claim 10, wherein the lipase is immobilized on a carrier, and the substrate of the carrier comprises chitosan.

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