Waste vinasse drying treatment system and method

Abstract

The invention relates to a waste vinasse drying treatment method. The method comprises the following steps: carrying out mechanical pressure filtration on original waste vinasse provided in batches in a solid-liquid separation manner; dehydrating the waste distiller's grains in a manner of removing moisture in the waste distiller's grains and gas influencing the caking rate; and screening the high-fiber waste vinasse and the heated and dehydrated waste vinasse separated from the organic matter-enriched waste vinasse based on a protein content differential separation mode to obtain oversize products for pyrolysis and undersize products for feed. According to the method, more moisture is reserved in the waste distiller's grains with high caking rate in mechanical filter pressing, the water in the waste distiller's grains can enable the waste distiller's grains to be agglomerated more easily, meanwhile, the high heat capacity characteristic of water can provide more uniform heat conduction for the waste distiller's grains, and the situation that the internal and external dehydration uniformity is not uniform due to local overheating of the waste distiller's grains is avoided.

Description

Technical Field

[0001] The present invention relates to the field of wine making, and in particular to a system and method for drying spent grains. Background Art

[0002] Winemaking spent grains are solid byproducts of solid-state liquor brewing. In the actual production process, the output ratio of liquor to spent grains is 1:3-4, that is, for every ton of liquor produced, 3-4 tons of spent grains will be produced. Untreated spent grains have the characteristics of high output, large amount of organic acid ester residues, high acidity, easy to mold, and high moisture content. Therefore, spent grains need to be treated before they can be discharged or pyrolyzed to reduce the pollution to soil, water and air.

[0003] The waste dregs drying device used in the prior art generally directly feeds the waste dregs into a feeder, heats it with a hot air blower, and dries it in a drying chamber. The inventors found that direct drying and pyrolysis have the following problems:

[0004] The particle size of high-water content waste grains is 1-6mm, which is sticky and easy to agglomerate. Direct heating and dehydration will often be affected by temperature and result in dry surface and wet inside.

[0005] The spent grains contain rich protein components, and the pyrolysis process will produce sulfides and nitrogen oxides, and the cost of pyrolysis tail gas treatment is relatively high.

[0006] Furthermore, the inventor explored the energy consumption of the dried lees by a single heating method, and explored the combination of multiple heating methods under the condition of single heating. Taking mechanical dehydration and heating dehydration as examples, the inventor explored the effect of mechanical dehydration and heating dehydration on the dried lees. The results showed that:

[0007] As the water content decreases, the energy consumption of mechanical dehydration increases approximately exponentially. When the water content of the spent grains decreases from 60% to between 35% and 40%, mechanical dehydration has significantly low energy consumption, and the process is simple and easy to handle. However, even if the mechanical action intensity is significantly increased, it is still difficult to reduce the water content of the spent grains to below 25%. The decrease in the water content of the spent grains under heating dehydration is positively correlated with the increase in energy consumption, and the slope of the curve is low, approximately a straight line. Heating dehydration can reduce the water content of the spent grains to below 10%. When the inventors conducted an energy consumption study by combining heating dehydration and mechanical dehydration, they found that taking the spent grains with a water content of less than 10% as the target for pyrolysis, and combining heating dehydration and mechanical dehydration for spent grain dehydration treatment can effectively reduce the energy consumption of the dehydration and drying process.

[0008] At the same time, the inventors found that in the process of processing different batches of dregs, even with the same process and preset processing parameters, the residual amount of dregs in the equipment and the screened material obtained after screening for pyrolysis will still generate high energy consumption during pyrolysis, and the crude protein content of the screened material separated is quite different. After long-term observation, the inventors found that the agglomeration rate of different batches of dregs before dehydration treatment becomes a key factor in the dehydration and screening process, and the dregs with different agglomeration rates due to the influence of ingredients and environment are treated differently in the feeding time and treatment process of mechanical filtration and heating dehydration to reduce the dehydration energy consumption, increase the crude protein content of the screened material, and increase the dispersion of the screened material (used to improve the pyrolysis efficiency).

[0009] In addition, on the one hand, there are differences in understanding among those skilled in the art; on the other hand, the applicant studied a large number of documents and patents when making the present invention, but due to space limitations, not all details and contents are listed in detail. However, this does not mean that the present invention does not have the characteristics of these prior arts. On the contrary, the present invention already has all the characteristics of the prior art, and the applicant reserves the right to add relevant prior art to the background technology. Summary of the invention

[0010] One of the purposes of the present invention is to provide a method and system for reducing the energy consumption of dehydrating spent grains.

[0011] One of the purposes of the present invention is to provide a method and system for improving the quality of spent grains as feed or feed additive.

[0012] One of the purposes of the present invention is to provide a method and system for reducing waste gas pollution during pyrolysis of spent grains.

[0013] One of the purposes of the present invention is to provide a method and system for treating waste grains to reduce particle size diameter.

[0014] One of the purposes of the present invention is to provide a method and system for reducing the risk of agglomeration during the dehydration of spent grains.

[0015] One of the purposes of the present invention is to provide a method and system for reducing the agglomeration rate during the dehydration process of spent grains.

[0016] One of the purposes of the present invention is to provide a processing method and system for reducing energy consumption during pyrolysis of spent grains.

[0017] Prior art has presented a technical solution for dehydrating wine lees by heating. For example, CN116809611A discloses a recycling method for white wine lees, first drying the lees, then screening the lees after drying into light waste and heavy residue, then packing the heavy residue for storage and other use, performing anoxic pyrolysis on the light waste and recovering solid residue, gas-liquid product and heat energy respectively, and finally purifying the gas-liquid product to discharge and complete the recycling of white wine lees. However, in this technical solution, only heating and dehydration mode is involved, and the reduction of water content of the lees under heating and dehydration is positively correlated with the increase of energy consumption, which means that a large amount of energy needs to be consumed in the dehydration process, resulting in increased costs. Traditional heating and dehydration methods, such as Tianguo steamer, have problems such as high labor intensity, unstable cooling effect, and low heat exchange efficiency, resulting in low production efficiency.

[0018] According to one aspect of the present invention, the present invention relates to a processing method and system for reducing the energy consumption of waste dregs dehydration, in particular, a waste dregs drying processing method, comprising the following steps: pre-treating the waste dregs to remove surface moisture; using at least one stage, preferably two stages or more preferably a multi-stage drying system to gradually reduce the moisture content of the waste dregs. Here, the drying temperature and humidity are precisely controlled to optimize energy consumption and dehydration efficiency. Here, when the waste dregs provided have a first moisture content, the working temperature of the dehydration device (paddle type) is set to the first temperature, and the dehydration is carried out at a constant temperature of the first temperature in the dehydration device (paddle type) until the second moisture content, and then the temperature is raised from the first temperature until the waste dregs reach a third moisture content; if the third moisture content has not been reached by the critical point of combustion, constant temperature dehydration is carried out at a temperature before the critical point of combustion until the third moisture content is reached. Here, when the working temperature of the dehydration equipment (paddle type) is set to the first temperature according to the moisture content of the pretreated waste, the relevant parameters characterizing the agglomeration rate are also considered, especially the organic matter content (first parameter) previously determined according to the standard sample, the ratio of the agglomeration mass to the total sample mass (second parameter) and the equivalent pressure value of the stirring process (third parameter).

[0019] According to one aspect of the present invention, the present invention relates to a treatment method and system for reducing waste gas pollution during pyrolysis of spent grains, comprising the following steps: adding adsorbents to capture harmful gases during the pyrolysis process; using a multi-stage filtration system to remove particulate matter and harmful substances.

[0020] According to one aspect of the present invention, the present invention relates to a processing method and system for reducing the risk of agglomeration during the dehydration process of the spent grains, comprising the following steps: using stirring and drying technology to maintain a uniform distribution of the spent grains; and using vibrating screening equipment to further prevent agglomeration formation.

[0021] According to one aspect of the present invention, the present invention relates to a processing method and system for reducing energy consumption during pyrolysis of spent grains, comprising the following steps: pre-drying the spent grains by mechanical filter pressing before pyrolysis to reduce the initial moisture content; using a high-efficiency pyrolysis furnace to optimize thermal energy utilization; and using an intelligent control system to accurately adjust the pyrolysis temperature and time to improve energy efficiency.

[0022] The above aspects can be used in conjunction with each other or in parallel as long as there is no contradiction between them.

[0023] Preferably or additionally, the present application further relates to a method for drying the dregs, which may include the following steps: S1 mechanically filtering the original dregs provided in batches in a solid-liquid separation manner, wherein a first dregs with a water content different from each other and a second dregs with a water content different from each other are provided in a manner related to the relevant parameters for characterizing the agglomeration rate, wherein the first water content is greater than the second water content; S2 dehydrating the dregs in a manner of removing water and gas affecting the agglomeration rate from the dregs, wherein S2.1 for the dregs filtered to the first water content, at a first temperature corresponding to the relevant parameters for characterizing the agglomeration rate, Dehydration is performed at a constant temperature until a second moisture content is reached, and then the spent grits that have been dehydrated at a constant temperature to a second moisture content are subjected to temperature-raising dehydration, or S2.2 the spent grits that have been filtered to a second moisture content are subjected to temperature-raising dehydration, wherein the temperature-raising dehydration is performed starting from a first temperature corresponding to a parameter related to the characterization of the agglomeration rate, until a second temperature lower than the critical point of combustion of the spent grits is reached and the second temperature is maintained until the spent grits reach a third moisture content; S3 the spent grits that have been heated and dehydrated after separation of high-fiber spent grits and organic-enriched spent grits are screened in a differential separation method based on protein content to obtain an oversize material for pyrolysis and an undersize material for feed.

[0024] Preferably, when at least one parameter used to characterize the agglomeration rate of the original lost grains provided in batches exceeds or is equal to a preset first threshold value of the relevant parameter used to characterize the agglomeration rate, the original lost grains whose relevant parameter exceeds or is equal to the preset first threshold value are filtered to a first moisture content; wherein, when at least one parameter used to characterize the agglomeration rate of the original lost grains is lower than the preset first threshold value of the relevant parameter used to characterize the agglomeration rate, the original lost grains whose relevant parameter is lower than the preset first threshold value are filtered to a second moisture content.

[0025] In this application, the original waste grains refer to the untreated waste grains remaining after the completion of winemaking and no longer used for fermentation.

[0026] Unlike the prior art, the present invention can use mechanical dehydration and heating dehydration to dehydrate the spent grains at the same time, wherein corresponding dehydration methods are set according to different agglomeration rates of the spent grains, and different dehydration methods can constitute associated processing flows. Based on the above-mentioned distinguishing technical features, the problems to be solved by the present invention may include: how to reduce the energy consumption of drying spent grains of winemaking. Specifically, mechanical dehydration can remove part of the water in the spent grains in advance, reducing the energy consumption and time of subsequent heating dehydration. For example: reducing the water content in advance through mechanical dehydration can reduce the heat required in the heating dehydration process, thereby reducing the overall energy consumption.

[0027] Preferably, the mechanical filtration comprises the following steps: mechanically filtration the original dregs with a water content of 57-62% in a solid-liquid separation manner, the filtration pressure is 0.8-1.2 MPa, the water content of the dregs is reduced to 35-40%, the filtrate is discarded, and the dregs are collected. Heating dehydration comprises the following steps: dehydrating the dregs in a manner to remove water and gas that affects the agglomeration rate in the dregs until the water content of the dregs is reduced to 8-10%. Screening the dregs with a water content reduced to 8-10% in a differential separation method based on protein content to obtain the oversize for pyrolysis and the undersize for organic matter enrichment.

[0028] More preferably, the original slag with a water content of 57.6% is mechanically filtered by solid-liquid separation, and the filter pressure is 1.2 MPa, so that the water content of the slag is reduced to 35.9%, and the filtrate is discarded and the slag is collected. The slag is dehydrated under the treatment condition of heating at 180°C for 15 minutes, and the water content of the slag is reduced to 8.1%. The slag with a water content reduced to 8.1% is screened with 80 mesh to obtain the screened material for pyrolysis and the screened material with a crude protein content of not less than 7%.

[0029] Beneficial effects of this technical solution:

[0030] 1. The inventors have studied the pyrolysis of spent grains with a water content of up to 65%, and have determined a low-energy and high-efficiency drying system by combining experiments with a variety of dehydration methods. The system can also solve the problems of uneven pyrolysis and gas pollution.

[0031] Based on the energy consumption control experiment provided in Example 1, it can be known that using a mechanical method when treating waste grains with a high moisture content (about 60%) and using a heating method when treating waste grains with a low moisture content (35% to 40%) will play a significant role in reducing energy consumption. Therefore, the inventors set a moisture content standard for judging the transition from mechanical dehydration to heating dehydration to ensure that the energy consumption of the drying treatment technology combining mechanical dehydration with heating dehydration is not only significantly reduced compared to the energy consumption of a single drying treatment technology, but also can make it lower than the energy consumption of drying treatment in other moisture content ranges.

[0032] At the same time, based on the operational impact of spent grains dehydration, the applicant took into account the various dehydration equipment involved in the prior art, and based on the dehydration effect and energy consumption analysis of mechanical dehydration and heating dehydration, found that taking spent grains with a moisture content of less than 10% as the target of pyrolysis, combining mechanical dehydration and heating dehydration to reduce the moisture content of spent grains can effectively reduce the energy consumption of the dehydration and drying process (Example 1, Figure 1 ). Therefore, whether from the perspective of energy efficiency or large-scale application scenarios, mechanical dehydration combined with heating dehydration is a better choice in the operation of spent grains dehydration.

[0033] 2. Related research results show that the crude fiber content of the solid after the dried lees is more than 30%, and the crude fiber content mainly comes from the rice husk component added during fermentation. This part can produce pyrolysis gas through pyrolysis, and provide energy for production after combustion. However, the crude protein content of the solid after the dried lees is more than 7% (see Examples 2 to 5), and direct pyrolysis will cause more sulfides and nitrogen oxides to be produced during the pyrolysis and combustion process. Therefore, the current treatment of the lees must be sprayed, desulfurized and denitrified before it can be discharged after meeting the standards.

[0034] The extended processing time and the need for secondary purification of the treated products during the spent grains treatment process lead to increased spent grains treatment costs.

[0035] Considering that direct pyrolysis of spent grains will produce high levels of sulfides and nitrogen oxides due to the rich protein components, the spent grains processing process of the present application sets up a screening step, and the crude fiber and low protein content components (screened material) in the spent grains are screened out for subsequent pyrolysis, while the high-protein and low-fiber part (screened material) can be used in other fields. The present application screens the spent grains after dehydration and drying, and the screened upper layer of spent grains is mainly crude fiber components, and the protein content of this type of crude fiber components is extremely low. This part of the spent grains is burned to provide energy for production, and the tail gas treatment is easier, with fewer pollutants and lower costs.

[0036] 3. In the process of combining the two dehydration methods, the inventors found that due to the influence of the state of different batches of dregs, the dispersion degree of the screened material produced by the linear mechanical filter press-heated filter press setting process is unstable, and the screened material produced by some of the treated dregs still has the problem of inefficient pyrolysis. At the same time, the organic matter content of the screened material produced (the present application takes crude protein as an example) is relatively large, which makes it impossible to control the quality of the treated dregs when used as pyrolysis materials and feed additives. The dregs with a high agglomeration rate have high viscosity. After pressure compression, it is not only difficult to be stirred evenly by a stirring device, but also may further increase the dregs agglomeration rate in the process of reducing the water content. At the same time, the dregs with a high agglomeration rate are more likely to have dregs that cannot be broken up with a diameter exceeding a certain range. Such dregs will form solid lumps that are soft inside and dry outside during the dehydration process (cannot be broken up by simple shearing or stirring), which increases the difficulty of screening.

[0037] Compared with the waste grains processing process involved in the prior art, the present application proposes a differentiated processing process based on the requirements for some physical states of the waste grains in actual applications, and proposes relevant supporting equipment based on this.

[0038] The present application allows the spent grains with a high agglomeration rate to retain more water during mechanical filtration. On the one hand, the presence of water can help soften the spent grains during the heating process, making it easier to deagglomerate, thereby improving the efficiency of stirring the spent grains; on the other hand, the high heat capacity of water can provide more uniform heat conduction for the spent grains during the heating process, avoiding local overheating of the spent grains and uneven dehydration uniformity inside and outside.

[0039] Another aspect of the present application relates to a waste dregs drying treatment system. The waste dregs drying treatment system includes a mechanical module for mechanically filtering and dehydrating the original waste dregs. The waste dregs drying treatment system includes a first detection module for detecting at least one parameter of the original waste dregs for characterizing the agglomeration rate. The waste dregs drying treatment system includes a drying module for heating the waste dregs at a constant temperature or at an increased temperature. The waste dregs drying treatment system includes a screening module for screening the dried waste dregs.

[0040] According to a preferred embodiment, the dregs drying treatment system is configured as follows: the mechanical module mechanically filters the raw dregs provided in batches in a solid-liquid separation manner. When at least one parameter used to characterize the agglomeration rate of the raw dregs detected by the first detection module exceeds or is equal to a preset first threshold value of a relevant parameter used to characterize the agglomeration rate, the mechanical module filters the raw dregs whose relevant parameters exceed or are equal to the preset first threshold value to a first moisture content.

[0041] According to a preferred embodiment, the lost grains drying treatment system is configured as follows: when at least one parameter used to characterize the agglomeration rate of the original lost grains detected by the first detection module is lower than a preset first threshold value of the relevant parameter used to characterize the agglomeration rate, the mechanical module presses the original lost grains whose relevant parameters are lower than the preset first threshold value to a second moisture content, wherein the first moisture content is greater than the second moisture content.

[0042] According to a preferred embodiment, the wasted grains drying treatment system is configured as follows: the drying module dehydrates the wasted grains in a manner of removing moisture and gas that affects the agglomeration rate from the wasted grains, wherein, for the wasted grains filtered to a first moisture content, at a first temperature corresponding to a relevant parameter characterizing the agglomeration rate, the drying module performs constant-temperature dehydration on the wasted grains with the first moisture content until a second moisture content is reached, and then performs temperature-raising dehydration on the wasted grains that have been dehydrated to the second moisture content; or for the wasted grains filtered to a second moisture content, at a first temperature corresponding to a relevant parameter characterizing the agglomeration rate, the drying module performs temperature-raising dehydration on the wasted grains with the second moisture content.

[0043] According to a preferred embodiment, the spent grains drying treatment system is configured as follows: the screening module screens the heated and dehydrated spent grains separated from the high-fiber spent grains and the organic-enriched spent grains in a differential separation method based on protein content to obtain the overscreen material for pyrolysis and the underscreen material for feed.

[0044] Beneficial effects of this technical solution:

[0045] The present application adjusts the pressure regulation process in the filter press process and performs differentiated filter press treatments on the spent grains with different agglomeration rates, so that the spent grains can enter the dehydration process based on transpiration with different water contents, so that the spent grains with high agglomeration rates can retain more moisture and higher conductivity. During the stirring process, the spent grains with high agglomeration rates are more easily broken up due to the influence of high water content.

[0046] The agglomeration rate not only affects the filtering and drying processes, but also directly affects the quality of the final product. For products used as feed additives, the degree of agglomeration will affect their appearance, and excessive agglomeration may lead to poor product appearance, thereby reducing the market acceptance of the product. The present application significantly improves the quality of the spent grains as feed after dehydration. As shown in Examples 2 to 5, the spent grains drying method proposed in the present application can obtain organic aggregated particles with a crude protein content of up to 7% or more without crude fiber.

[0047] According to a preferred embodiment, the second detection module for detecting the moisture content of the original waste grains collects the moisture content b of the original waste grains and transmits it to the control unit, wherein the control unit calculates the first moisture content M1 by formula (1):

[0048] M1=b-k1×(A1-a) (1),

[0049] b represents the water content of the original waste; k1 represents a constant; A1 represents a related parameter that exceeds or is equal to a preset first threshold a; a represents the first threshold.

[0050] According to a preferred embodiment, in the processing step S1, the first water content M1 can be calculated by formula (1).

[0051] According to a preferred embodiment, the water content b of the original waste grains is collected in the second detection module for detecting the water content of the original waste grains and transmitted to the control unit, wherein the control unit calculates the second water content M2 by formula (2):

[0052] M2=b-k2×(a-A2) (2),

[0053] b represents the water content of the original waste; k2 represents a constant; A2 represents a related parameter lower than a preset first threshold a; a represents the first threshold.

[0054] According to a preferred embodiment, in the processing step S1, the second water content M2 can be calculated by formula (2).

[0055] Beneficial effects of this technical solution:

[0056] This application introduces the relationship between the agglomeration rate and the preset threshold value, so that the operator can dynamically adjust the specific value of the moisture content based on the formula, thereby achieving the purpose of accurately controlling the moisture content of the spent grains, and meeting the quality control of the spent grains in different batches for different application purposes or different factory states.

[0057] K1 in formula (1) and k2 in formula (2) both represent constants, which are used to optimize the calculation of moisture content. The staff can confirm the constant values ​​suitable for them according to different processing requirements or relevant experimental data.

[0058] The preset first threshold a is set manually according to an empirical table. Water content is an important factor affecting the agglomeration rate of the original waste lees. At the same time, different batches of original waste lees will also have different agglomeration rates due to factors such as the cellar, fermentation season, and raw materials. Based on this, the a value in formula (1) and formula (2) can be set according to the empirical table.

[0059] According to a preferred embodiment, in step S1, the mechanical module for mechanically filtering and dehydrating the original dregs exerts a squeezing effect on the original dregs by applying pressure, and discharges part of the liquid containing free water and capillary water through the pores of the solid matter in a manner that the solid matter in the original dregs is retained and transferred to a drying module for removing water in solid particles and gas that affects the agglomeration rate. The dregs agglomerates generated by polymerized proteins in the solid matter with free water as a medium are reduced by the above-mentioned filtering method. Preferably, the solid matter contains protein, plant fiber, microbial residues and microbial metabolic residues.

[0060] Beneficial effects of this technical solution:

[0061] Although simple extrusion, especially the extrusion method with continuously increasing pressure, can intercept solid matter in the original waste, it also forces part of the gas to increase its solubility in the liquid, and even forms lumps and locks a large number of bubbles and moisture in a large number of lumps. For this reason, in the process of mechanical filtration and dehydration of the original waste, the present invention applies pressure in a fluctuating manner, especially in a fluctuating manner of first high pressure and then low pressure, in order to reduce the aggregated protein lumps with free water as the medium, and prompts the mechanical module to stagger the high extrusion pressure points in time, so as to further reduce the aggregated protein lumps with free water as the medium, thereby eliminating the formation process of lumps containing water bubbles or bubbles.

[0062] The water locked in the mass exists in the form of free water, capillary water and bound water.

[0063] A liquid in the form of free water is, for example, a liquid that does not form strong interactions with solute molecules.

[0064] Liquid in the form of capillary water is, for example, liquid trapped in small pores or fibers inside a material by capillary action. Due to the influence of capillary action (i.e., surface tension and adhesion), liquid in the form of capillary water needs to overcome the forces between it and the solid material in order to be discharged. Therefore, even if the pressure is increased, some of the liquid in the form of capillary water with a larger force between it and the solid material will still remain in the solid material.

[0065] Since the solid matter in the waste contains more fibers, when separating the liquid and solid, the liquid in the form of free water retained in the solid agglomerates will be separated first. Considering that the energy consumption of mechanical filter pressing is much lower than that of heated filter pressing, the liquid in the form of free water in the waste is squeezed out through the pores in the solid matter (especially the agglomerates of solid matter) through mechanical filter pressing. At the same time, during the process of applying pressure, some liquid in the form of capillary water will also be squeezed out.

[0066] The waste contains a high proportion of water (usually between 60% and 80%) and also includes unfermented starch, protein, cellulose, fat and microbial cells. As the water content in the waste gradually decreases, the difference in agglomeration rate will gradually increase, and the unfermented starch, protein, cellulose and other components contained therein will also form a water-absorbing network and become a factor that hinders the dehydration of the waste. At the same time, as the water is lost, the part of the waste that is condensed into agglomerates or blocks will gradually become compact and cannot be easily broken up (as the water is removed, the distance between the solid particles in the agglomerated or blocky waste decreases, such as unfermented starch, protein, cellulose, etc., which are in closer contact with each other; the removal of water reduces the lubrication between the particles, so that the friction and bonding force between the solid particles are enhanced; some chemical changes that increase the firmness of the waste may also occur during the dehydration process, including protein denaturation and starch gelatinization).

[0067] The combination of different forms of solids and liquids in the grits will have a significant effect on the grit agglomeration rate and how to reduce the grit agglomeration rate. Liquid in the form of free water can be discharged through a simple mechanical filter press. When the pressure of the mechanical filter press increases, that is, when the external squeezing effect is enhanced, some of the liquid in the form of capillary water will also be discharged after overcoming the force formed between it and the solid matter. The discharge of the above liquid can reduce the aggregation between the solid substances containing protein in the grits, thereby reducing the grit agglomeration rate. For example: if the content of liquid in the form of free water is reduced, the intermediate substances that can support the polymerization between proteins can be reduced, so that more proteins are dispersed in the grits in the form of monomers. Unlike the effect of reticulated proteins on grits, the presence of monomeric proteins has a lower degree of influence on grit agglomeration, and also makes the grits that become filter cakes due to external squeezing easier to be broken up during the stirring process.

[0068] According to a preferred embodiment, the drying module provides heat to the waste grits which are transported after filtration by the mechanical module and are at a first moisture content or a second moisture content due to the capillary water and bound water present therein, and dehydrates the waste grits with the first moisture content in a manner of reducing the agglomeration rate of the waste grits by removing the capillary water and bound water distributed in the solid matter in the waste grits.

[0069] Beneficial effects of this technical solution:

[0070] Under the traditional treatment method, since a large number of bubbles and water are locked in a large number of agglomerates, the agglomerates cannot release the water and gas therein until the combustion critical value or even higher temperature, and may even form a hydration reaction related to protein modification. To this end, according to the present invention, the waste dregs at the first water content after the filter pressing process will be stirred at a high speed before being heated to the first temperature, especially during the feeding period, the stirring speed is faster than the stirring speed during the final heating and dehydration period, that is, before feeding, the stirring speed of the drying module is set to a higher stirring speed, so that the agglomerates locked with a large number of bubbles and water can be mechanically dispersed by mutual collision during the feeding stage, avoiding the half-barrel effect caused by the downward deposition of the agglomerates under the action of gravity, that is, the high-water content agglomerates under pressure will accumulate in the lower part and continue to accumulate in the lower half stirring interval at high temperature, and together form a "shell" formed by the waste dregs facing the stirring mechanism, and this shell will form a thermal insulation layer, causing a large amount of ineffective energy consumption. According to the present invention, the "waste transferred after filtration" is at the first moisture content or the second moisture content due to the influence of capillary water and bound water present therein, and the feeding speed or the feeding speed change rate is pre-set according to both the stirring speed and the moisture content (first or second).

[0071] At the same time, during the heating process, a large amount of liquid in the form of bound water in the agglomerate will also contact the high temperature environment before the first temperature (including the first temperature) based on the shearing effect generated by stirring, thereby improving the utilization efficiency of the high temperature environment. Liquid in the form of bound water is, for example, a liquid that forms a strong interaction with solute molecules, ions or other components. This type of liquid is tightly bound to the solute through hydrogen bonds, ion-dipole interactions or other chemical bonds, and this combination usually changes the physical and chemical properties of water. For example: in the waste dregs, the liquid can form hydrogen bonds with the polar groups on the surface of the protein (one of the solid substances) in the waste dregs to become bound water. The present application is based on heating and dehydration to increase the ambient temperature to destroy the chemical bonds formed between the liquid in the form of bound water and the protein in the waste dregs, and based on energy accumulation to evaporate the liquid, so that the polymerized protein is distributed in the waste dregs in the form of free amino acids or monomeric proteins. Free water as an intermediate medium connects multiple monomeric proteins through chemical bonds to form polymerized proteins. After the connection between free water and protein, free water is converted into bound water. Most of the polymerized proteins are in a network shape, which increases the viscosity of the waste dregs and improves the agglomeration rate of the waste dregs.

[0072] The technical solution provides high temperature conditions, which affect the solubility and viscoelasticity of proteins by means of protein deformation and chemical bond destruction, and increase the possibility of deformed proteins aggregating in the form of large particles (rather than a mesh), so that the undersize material during the screening process can retain as much crude protein as possible, rather than being attached to the fiber surface of the oversize material in the form of free polypeptides or amino acids.

[0073] According to a preferred embodiment, the mechanical module mechanically filters the original waste grains in a manner of a preset first threshold value of a relevant parameter for characterizing the agglomeration rate updated for each batch and according to the process parameters affecting the agglomeration rate for each batch.

[0074] Preferably, the process parameters affecting the agglomeration rate include but are not limited to the type of cellar, the water content of the original spent lees, the time of production of the spent lees (which can be accurate to the day), the application type of Daqu, the raw materials of the fermented grains, and the pH value of the original spent lees. The specific operation of adjusting the first threshold value according to the process parameters can be referred to Example 10.

[0075] Beneficial effects of this technical solution:

[0076] 1. Each batch of spent lees is individually set with relevant parameters for spent lees produced in different seasons. These parameters are recorded in a manner related to the corresponding cellar number. The parameters used to characterize the agglomeration rate are related to the quality of the spent lees, and these parameters are also conducive to reversely indicating the degree of fermentation. These parameters stored in relation to the corresponding cellar number can be used to improve the timing of feeding and opening the cellar after many years of continuous production.

[0077] 2. By collecting and analyzing the process parameter data related to the agglomeration rate, a more accurate data model can be established, reducing the manual intervention in the setting of the first threshold value for different batches of lees. The process parameters affecting the agglomeration rate are used as independent variables, and the selection of the first threshold value of the parameters related to the agglomeration rate as the dependent variable is more targeted in each batch, so that the setting of the first threshold value is more closely related to the agglomeration rate it represents, so that the dynamic adjustment of the process parameters can not only reduce the agglomeration rate of the lees during the processing process, but also maintain the consistency and stability of the quality of the lees after processing (such as crude protein content).

[0078] According to a preferred embodiment, the relevant parameters for characterizing the agglomeration rate include a second parameter calculated from the mass of the agglomerated portion and the total sample mass, and the second parameter is calculated by formula (3):

[0079]

[0080] Beneficial effects of this technical solution:

[0081] The mass of the agglomerated part and the total sample mass are used as evaluation parameters, which reduces the difficulty of obtaining the relevant parameters used to characterize the agglomeration rate, making the technical solution more suitable for factory or workshop operations. Compared with more complex chemical analysis methods, the parameters obtained by visual inspection, image acquisition or screening weighing reduce the complexity of obtaining the second parameter and increase the measurement efficiency of the second parameter.

[0082] According to a preferred embodiment, in the processing step S1, the relevant parameter characterizing the agglomeration rate may be the organic matter content. The first detection module is configured as a relevant device for detecting the organic matter content. The first threshold may be set to a numerical value of the organic matter content. Preferably, the first threshold is set between a mass fraction of 5 and 50%. More preferably, the first threshold is set to a mass fraction of 20%.

[0083] According to a preferred embodiment, at least one parameter for characterizing the clumping rate is set to a first parameter representing the organic matter content, wherein when the first parameter exceeds or is equal to a preset first threshold value, the mechanical module for mechanically pressing and dehydrating the original lost grains presses the original lost grains whose first parameter exceeds or is equal to the preset first threshold value to a first moisture content calculated by the control unit according to formula (1); when the first parameter is lower than the preset first threshold value, the mechanical module presses the original lost grains whose first parameter is lower than the preset first threshold value to a second moisture content calculated by the control unit according to formula (2).

[0084] Preferably, the first detection module is configured to detect the organic matter content of the original waste dregs, wherein, when the organic matter content detected by the first detection module exceeds or is equal to a preset first threshold value of the organic matter content, the mechanical module presses the original waste dregs whose organic matter content exceeds or is equal to the preset first threshold value of the organic matter content to a first water content calculated by the control unit according to formula (1); when the organic matter content detected by the first detection module is lower than the preset first threshold value of the organic matter content, the mechanical module presses the original waste dregs whose organic matter content is lower than the preset first threshold value of the organic matter content to a second water content calculated by the control unit according to formula (2).

[0085] Beneficial effects of this technical solution:

[0086] Factors affecting the clumping rate include:

[0087] (1) Moisture content: Higher moisture content usually increases the stickiness and agglomeration tendency of the grains, while lowering the moisture content helps reduce the amount of grains agglomeration.

[0088] (2) Organic matter content: Protein polymerization will form a network of high molecular weight structures, which may affect the viscosity of the lees and thus the agglomeration rate. In addition, high temperature may cause protein modification, making the lees more viscous, which further affects the agglomeration rate.

[0089] (3) Pressure during mechanical filtration: The continuous pressure exerted on the spent grains by the filtration-press dehydration equipment will lead to an increase in the agglomeration rate of the spent grains.

[0090] Considering that water will be lost during the dehydration process and the proportion of free water will decrease, the content of organic matter that persists in the waste lees as a relevant parameter for evaluating the agglomeration rate of the waste lees can increase the stability of the evaluation results. At the same time, since the detection accuracy of the organic matter content is high (it needs to be measured with a high-precision instrument), the accuracy of the agglomeration rate represented by it is also high.

[0091] According to a preferred embodiment, in the processing step S1, the relevant parameter characterizing the agglomeration rate can be a third parameter represented by a pressure value. Preferably, the first detection module is set to a stirring pressure rod, and the agglomeration rate of the waste dregs is characterized by the pressure value (i.e., the third parameter) displayed by the stirring pressure rod during the stirring process of the waste dregs. Preferably, the first threshold value can be set as a pressure parameter. Preferably, the first threshold value is set between 50 and 70 mPa.s. More preferably, the first threshold value is set to 60 mPa.s.

[0092] According to a preferred embodiment, in the processing step S2, the dehydration treatment includes the following steps: using the water content of the lees reduced to a third water content that can be used as dry feed as a judgment basis for stopping the dehydration treatment, and performing a dehydration treatment from the first temperature to a preset maximum temperature value on the lees whose water content is reduced to the second water content and is filtered to the first water content or the lees whose water content is filtered to the second water content. According to the processing method described in Examples 2 to 5, the lees with a water content of less than 20% after the final dehydration can be screened, and a screened material with a crude protein content of not less than 7% can be obtained.

[0093] In the processing step S1, the original waste grains provided in batches and having at least one parameter characterizing the agglomeration rate exceeding or equal to a preset first threshold value of the relevant parameter characterizing the agglomeration rate are mechanically filtered with gradient pressure.

[0094] Beneficial effects of this technical solution:

[0095] Different from the prior art, the present invention can evaluate the agglomeration rate of the original dregs according to the relevant parameters detected by the first detection module, and dynamically adjust the filter press parameters of the filter press based on the detection results. Based on the above-mentioned distinguishing technical features, the problems to be solved by the present invention may include: how to reduce the probability of dregs agglomerating or lumping during the filter press dehydration process. Specifically, in the traditional filter press dehydration process, since the agglomeration rate of the dregs gradually increases as its water content decreases, this greatly increases the possibility of the dregs agglomerating or lumping during the filter press process. If a unified filter press parameter is used to treat dregs with different agglomeration rates, the dregs with a larger agglomeration rate will be more likely to agglomerate or agglomerate. This agglomeration or agglomeration will not only affect the subsequent drying effect, but may also cause the dried dregs feed to have a block or agglomerate structure with increased firmness and hardness, thereby affecting its quality and applicability as a feed.

[0096] Compared with the gradual filter press, the stage filter press can also reduce energy consumption and reduce the mechanical loss of the filter press. The gradual filter press needs to continuously overcome the flow resistance of the waste to increase the pressure during the filtration process, while the stage filter press keeps the pressure constant in each stage. Therefore, the equipment in the stage filter press does not need to be in the state of boosting and changing pressure for a long time, which also reduces the loss of equipment and energy consumption.

[0097] According to a preferred embodiment, in the processing step S1, based on the gradually increasing pressure provided, the original waste grains provided in batches and having at least one parameter characterizing the agglomeration rate lower than a preset first threshold value of the relevant parameter characterizing the agglomeration rate are continuously mechanically filtered by solid-liquid separation.

[0098] Beneficial effects of this technical solution:

[0099] Considering that the risk of increasing agglomeration rate of the waste with low agglomeration rate after the water content decreases is relatively low, a gradual filter pressing procedure is adopted. The pressure gradually increases during the gradual filter pressing process, which helps to discharge the water in the waste more evenly. However, due to the gradual increase in pressure, the structure of the waste in the form of filter cake after filtration may be more uniform and the density may be higher. Therefore, for the waste with relatively low agglomeration rate, considering that the agglomerated or lumped waste produced during the mechanical filter pressing process is easy to be broken up in the drying module or agitator, the filter press is set to the gradual filter pressing procedure for the purpose of increasing the waste drainage efficiency and reducing energy consumption.

[0100] According to a preferred embodiment, in the treatment step S3, the crude protein content in the organic matter-enriched waste is not less than 7%. According to Examples 2 to 5, the crude protein content of the undersize obtained by the treatment methods provided in Examples 2 to 5 is not less than 7%.

[0101] According to a preferred embodiment, the first moisture content ranges from 40% to 50%. Preferably, the first moisture content is 50%, 45% or 40%.

[0102] According to a preferred embodiment, the second moisture content ranges from 30% to 40%. Preferably, the second moisture content is 30%, 40% or 35%.

[0103] Preferably, the mechanical module is configured as a plate-frame filter press. The specific operation steps of the mechanical module for mechanically filtering the original waste dregs provided in batches in a solid-liquid separation manner are, for example: the plate-frame filter press filters the waste dregs with a water content of 57-62% at a pressure of 0.8-1.2 MPa, reducing the water content of the waste dregs to 35-40%, discarding the filtrate, and collecting the waste dregs filter cake.

[0104] Preferably, the drying module comprises a paddle dryer. The specific operation steps of the drying module for dehydrating the spent grits by removing the water in the spent grits and the gas that affects the agglomeration rate are, for example: the spent grits filter cake is transferred to the paddle dryer, heated and dehydrated until the water content of the spent grits is reduced to 8-10%; the spent grits with a water content reduced to 8-10% are sieved to obtain the oversize for pyrolysis and the undersize for enriching organic matter.

[0105] More preferably, the plate and frame filter press is used to filter the waste dregs with a water content of 57.6%, the filter pressure is set to 1.2 MPa, and the waste dregs are filtered until the water content reaches 35.9%; the filtrate is discarded and the waste dregs filter cake is collected. The waste dregs after filtration are transferred to a paddle dryer, heated at 180°C for 15 minutes, and dehydrated until the water content of the waste dregs reaches 8.1%. The screening module screens the waste dregs with a water content of 8.1%.

[0106] According to a preferred embodiment, the dehydration temperature of the drying module ranges from 100 to 200° C. Preferably, the dehydration temperature of the drying module is 100° C., 110° C., 120° C., 130° C., 140° C., 150° C., 160° C., 170° C., 180° C., 190° C. or 200° C.

[0107] According to a preferred embodiment, the mesh size of the sieve used for screening is 60 to 80 meshes. Preferably, the mesh size is 60 meshes. Preferably, the mesh size is 70 meshes. Preferably, the mesh size is 80 meshes.

[0108] According to a preferred embodiment, the filter pressure ranges from 1 to 1.2 MPa. Preferably, the filter pressure is 1 MPa. Preferably, the filter pressure is 1.1 MPa. Preferably, the filter pressure is 1.2 MPa.

[0109] According to a preferred embodiment, the heating temperature of the paddle dryer ranges from 160 to 200° C. Preferably, the heating temperature of the paddle dryer is 160° C. Preferably, the heating temperature of the paddle dryer is 180° C. Preferably, the heating temperature of the paddle dryer is 200° C.

[0110] According to a preferred embodiment, the heating time of the paddle dryer ranges from 10 to 15 minutes. Preferably, the heating time of the paddle dryer is 10 minutes. Preferably, the heating time of the paddle dryer is 15 minutes.

[0111] Preferably, the first time length is shorter than the second time length. For example, if the first time length is 15 minutes, the second time length may be 20 minutes.

[0112] Preferably, the first pressure value is selected from 0.1 to 0.5 MPa. More preferably, the first pressure value is 0.1 MPa. The first pressure value is 0.2 MPa. The first pressure value is 0.3 MPa. The first pressure value is 0.4 MPa. The first pressure value is 0.5 MPa.

[0113] Preferably, the second pressure value is selected from 0.5 to 1.0 MPa. More preferably, the second pressure value is 0.5 MPa. The second pressure value is 0.6 MPa. The second pressure value is 0.7 MPa. The second pressure value is 0.8 MPa. The second pressure value is 0.9 MPa. The second pressure value is 1.0 MPa.

[0114] Preferably, the third pressure value is selected from 0.5 to 1.5 MPa. More preferably, the third pressure value is 0.8 MPa. The third pressure value is 1.0 MPa. BRIEF DESCRIPTION OF THE DRAWINGS

[0115] Figure 1 Energy consumption statistics provided by the present invention;

[0116] Figure 2 A process flow chart of step S1 provided by the present invention;

[0117] Figure 3 The process flow chart of step S2 provided by the present invention. DETAILED DESCRIPTION

[0118] The following is a detailed description with reference to the accompanying drawings.

[0119] In the description of the present invention, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance. "Several" means two or more, unless otherwise clearly and specifically defined. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0120] Agglomeration rate is a method to characterize the performance of sticky mash (e.g., fermented mash) during the processing. Agglomeration rate usually refers to the degree to which mash forms lumps under certain conditions. For sticky mash, the determination and control of agglomeration rate is very important. Agglomeration may affect the solid-liquid separation efficiency, filtration rate and product quality. Agglomeration rate refers to the proportion of agglomerates formed between mash particles due to stickiness or other reasons during the processing. Agglomeration rate can be expressed by measuring the proportion of agglomerated parts in mash per unit volume or mass. For example, the agglomeration rate can be calculated by the following formula:

[0121]

[0122] The clumping rate can be measured by:

[0123] 1. Sieving method: Use a series of standard sieves to pass part of the sample through sieves of different particle sizes to separate the agglomerated part and the non-agglomerated part.

[0124] 2. Manual separation method: Manually separate the sample into agglomerated and non-agglomerated parts, weigh them separately and calculate the agglomeration rate.

[0125] 3. Visual identification or image analysis: roughly estimate the proportion of the agglomerated part by visual inspection of the sample or through image analysis.

[0126] Example 1

[0127] Mechanical methods are used to treat waste grains with high moisture content (about 60%), and heating methods are used to treat waste grains with low moisture content (35% to 40%).

[0128] Paddle dryer (KJG-300, heat transfer area 300m 2 ) and plate and frame filter press (specification model XAMG80 / 1000-30U, filtration pressure 0.6~1.2MPa, filtration area 80m 2 , filter plate size 1000mm*1000mm) as an example.

[0129] The plate and frame filter press consumes 50k of electric energy to reduce the water content of 70% waste to 40% at a pressure of 1.0Mpa. The paddle dryer consumes 80k of electric energy to reduce the water content of 70% waste to 40% at a heating temperature of 160°C. Based on the calculation of electric energy consumption, the electric energy loss is calculated in the three methods of reducing the waste from 70% to 20% in this embodiment.

[0130] like Figure 1 As shown, in the process of gradually decreasing the moisture content of the spent grains (especially after 40%), the energy consumption of the mechanical drying method directly increases from 50k (moisture content 40%) to 400 (moisture content 20%), and the energy consumption of the heating drying method directly increases from 80k (moisture content 40%) to 150 (moisture content 20%), and the energy consumption of the combined mechanical and heating drying method increases from 50k (moisture content 40%) to 100 (moisture content 20%).

[0131] The results show:

[0132] When mechanical dehydration is used, energy consumption increases approximately exponentially with decreasing water content. Mechanical dehydration has significantly low energy consumption when the water content of the spent grains is reduced to between 35% and 40% with a water content of about 60%. However, even if the mechanical action intensity is significantly increased, it is still difficult to reduce the water content of the spent grains to below 25% (line A).

[0133] When heating dehydration is used, the decrease in water content and the increase in energy consumption are positively correlated, and the slope of the curve is low, approximating a straight line. Although heating dehydration can reduce the water content of the spent grains to below 10%, as the water content of the spent grains decreases, the energy consumption required for heating dehydration also gradually increases (line B).

[0134] When mechanical dehydration and thermal dehydration are used in combination, that is, mechanical method is used when treating waste grains with high moisture content (40%-60%), and thermal method is used when treating waste grains with low moisture content (35%-40%), energy consumption is significantly reduced (line C).

[0135] At present, the main way to use spent grains is to use them as feed additives after drying and deacidification. In recent years, the use of pyrolysis to convert high-water spent grains into steam and other energy and biochar required for the brewing process has become a research hotspot due to its fast, clean, and large-scale processing characteristics. Many studies have shown that when the water content of solid waste is reduced from 80% to 30%, the required heat will increase from 70 kcal / kg to 2400 kcal / kg. According to relevant reports, when a chain furnace is used to treat spent grains produced by brewing, waste with a high water content cannot be completely pyrolyzed and burned in the furnace. The above results show that the moisture content of solid waste has a significant effect on its pyrolysis.

[0136] Example 2

[0137] This embodiment provides a specific implementation method for waste grains treatment without using mechanical filtration.

[0138] The steps of waste disposal include:

[0139] (1) collecting solid-state liquor waste and determining the water content to be 57.6%;

[0140] (2) sending the liquor lees into a paddle dryer at a temperature of 180°C for 28 minutes until the water content of the lees is reduced to 9.8%;

[0141] (3) The dried dregs in (2) were sieved and passed through an 80-mesh sieve. The sieved material was collected and the protein content was determined to be 7.0%.

[0142] Example 3

[0143] This embodiment provides a specific implementation method for treating the spent grains. Unlike the above embodiments, this embodiment does not include screening the spent grains after drying.

[0144] (1) collecting solid-state liquor waste and determining the water content to be 57.6%;

[0145] (2) Using a plate and frame filter press to filter the waste dregs, the equipment pressure is 1.2 MPa, the filtrate is discarded, and the waste dregs filter cake is collected. The water content is measured to be 35.9%;

[0146] (3) The waste cake was sent to a paddle dryer at an operating temperature of 180°C for 15 minutes. The moisture content of the waste cake was reduced to 8.5%, and the protein content was measured to be 17.6%.

[0147] Example 4

[0148] This embodiment provides a specific implementation method for waste dregs processing. Unlike the above embodiments, the processing method of this embodiment optimizes the processing parameters.

[0149] (1) Collecting solid-state liquor waste and measuring the water content to be 61.8%;

[0150] (2) Using a plate and frame filter press to filter the waste dregs, the equipment pressure is 1 MPa, the filtrate is discarded, and the waste dregs filter cake is collected. The water content is measured to be 36.8%;

[0151] (3) The waste cake was sent to a paddle dryer at a temperature of 160°C for 15 minutes, and the water content of the waste cake was reduced to 9.8%. The protein content was measured to be 16.8%.

[0152] (4) The dried dregs from (3) were sieved and passed through a 60-mesh sieve. The sieved material was collected and the protein content was determined to be 7.2%.

[0153] Example 5

[0154] This embodiment provides a specific implementation method for waste dregs processing. Unlike the above embodiments, the processing method of this embodiment optimizes the processing parameters.

[0155] (1) Collecting solid-state liquor waste and measuring the water content to be 61.8%;

[0156] (2) Using a plate and frame filter press to filter the waste dregs, the equipment pressure is 1 MPa, the filtrate is discarded, and the waste dregs filter cake is collected. The water content is measured to be 36.8%;

[0157] (3) The waste cake was sent to a paddle dryer at an operating temperature of 180°C for 12 minutes, and the water content of the waste cake was reduced to 9.5%. The protein content was measured to be 16.8%;

[0158] (4) The dried dregs from (3) were sieved and passed through a 60-mesh sieve. The sieved material was collected and the protein content was determined to be 7.1%.

[0159] Example 6

[0160] The present application relates to a drying process and system for waste waste with obvious particle aggregation. The contents repeated in the above embodiments are omitted. As long as there is no contradiction, the following technical features are applicable to the above embodiments, and vice versa.

[0161] The steps of S1 include:

[0162] S1-1 confirms the first threshold a and constant k1 of the current batch of samples based on the empirical table, and measures the moisture content b of the original waste;

[0163] S1-2 Determine at least three sampling points of the original dregs, weigh the total mass of the original dregs at the sampling points within the determined range and the mass of the agglomerated part after screening, and obtain the parameter A1 of the original dregs based on the following formula:

[0164]

[0165] S1-3 obtains the first water content M1 based on the following formula (1):

[0166] M1=b-k1×(A1-a) (1),

[0167] b represents the water content of the original waste; k1 represents a constant; A1 represents a parameter that exceeds or is equal to a preset first threshold; a represents the first threshold;

[0168] S1-4 When the parameter A1 used to characterize the agglomeration rate of the original waste provided in batches exceeds or is equal to the preset first threshold value a of the relevant parameter used to characterize the agglomeration rate, the original waste whose parameter A1 exceeds or is equal to the preset first threshold value a is mechanically filtered to a first moisture content M1 in a solid-liquid separation manner.

[0169] According to a preferred embodiment, the original slugs provided in batches and having a parameter A1 characterizing the agglomeration rate exceeding or equal to a preset first threshold value of a relevant parameter characterizing the agglomeration rate are mechanically filtered with a gradient pressure change.

[0170] According to a preferred embodiment, the steps of mechanical filtration of the original waste with parameter A1 exceeding or equal to the preset first threshold value a include: S1-4-1 pulse pre-pressure filtration stage, S1-4-2 main pressure filtration stage, S1-4-3 high-pressure filtration stage, S1-4-4 pulse high-pressure filtration stage.

[0171] Preferably, S1-4-1 pulse pre-pressure filtration stage: the mechanical module provides initial filtration for the waste in the mechanical module at a set first pressure value.

[0172] The purpose of the pre-pressure filtration stage is to initially discharge the free water in the waste and form a preliminary filter cake structure. The waste is evenly distributed on the filter cloth (or filter frame) through low-pressure filtration.

[0173] Preferably, as shown in Table 1, Figure 2 As shown, S1-4-2 is the main pressure filtration stage: the mechanical module filters the waste in the mechanical module at a set second pressure value. More preferably, the main pressure filtration stage includes high-pressure stages with different filtration durations and pressures. For example: S1-4-2-1 The mechanical module filters the waste in the mechanical module at a set second pressure value in the first stage within a preset first time length; S1-4-2-2 The mechanical module filters the waste in the mechanical module at a set second pressure value in the second stage within a preset second time length. The second pressure value in the first stage is greater than the second pressure value in the second stage. For example: 1.0Mpa continuous filtration, switch to 0.5Mpa after 5 minutes, switch to 1.0Mpa continuous filtration after 5 minutes, switch to 0.5Mpa after 5 minutes, and the above filtration process is repeated 3 times.

[0174] Preferably, S1-4-4 pulse high-pressure filtration stage: the mechanical module applies short-term pressure to the waste grains in the filter press mechanical module at least once with a set third pressure value until the water content of the waste grains in the mechanical module is less than the first water content.

[0175] The waste drying system further comprises a control unit provided with an input terminal and having a computing capability. The control unit is configured to: confirm the first threshold a and the constant k1 based on an experience table inputted into the input terminal of the control unit or a selection instruction of an experience table pre-stored in the control unit.

[0176] The control unit is configured to calculate a parameter A1 representing the agglomeration rate of the current batch of the scraps based on the total mass m1 (i.e., the total sample mass) of the scraps transmitted by the first detection module and the mass m2 of the agglomerated scraps (i.e., the mass of the agglomerated portion) of the scraps by the following formula (4):

[0177]

[0178] The control unit is configured to obtain the first moisture content M1 by the following formula (1) based on the acquired A1, the moisture content b of the original waste transmitted by the second detection module, the constant k1, and the first threshold a:

[0179] M1=b-k1×(A1-a) (1),

[0180] b represents the water content of the original waste; k1 represents a constant; A1 represents a parameter characterizing the agglomeration rate that exceeds or is equal to a preset first threshold; a represents the first threshold.

[0181] The first detection module is configured to collect the dregs at manually confirmed sampling points or randomly generated sampling points, and weigh the total mass m1 of the dregs and the mass m2 of the agglomerated dregs respectively.

[0182] The second detection module is configured to detect the water content b in the original waste grains.

[0183] The mechanical module is configured to: when A1 is not less than a, the original waste is filtered to a first moisture content M1 using the following filtering steps:

[0184] Pulse filter pressing with a preset first pressure value;

[0185] Filtering at a preset second pressure value within a preset first time length;

[0186] Filtering at a preset third pressure value within a preset second time length:

[0187] The third pressure value pulse filter is used, wherein the first time length is shorter than the second time length, and the second pressure value is larger than the third pressure value.

[0188] Preferably, the operation procedure of the waste drying system is as follows:

[0189] Input: first threshold a, constant k1, water content b of original waste;

[0190] The sampling volume of each sample point after random sampling is calculated using the following formula:

[0191]

[0192] rand(a, b) means generating a random number in the interval [a, b]. i is the mass of the i-th sampling point, the total volume of the original waste is M, and the number of sampling points to be selected is n (n≥3),

[0193] According to the random mass range generated by formula (4), samples m1 (i.e., the above m i ), and weigh the mass m2 of the agglomerated part after screening these samples;

[0194] Calculate the average agglomeration rate A avg :

[0195]

[0196] Calculate the first moisture content M1:

[0197] M1=b-k1×(A avg -a) (8);

[0198] The control mechanical module performs the following operations:

[0199] Pulse filter press with pressure P1;

[0200] During time T1, filter at pressure P2;

[0201] During time T2, filter at pressure P3;

[0202] Pulse filtration is performed at a pressure of P3 until the water content of the waste grains reaches a first water content M1, wherein T1 < T2 and P2 < P3.

[0203] Table 1

[0204] Filter pressing stage Filter pressing conditions (pressure-time) Pulse pre-pressure filtration stage <![CDATA[P1]]> Main pressure filtration stage <![CDATA[P2→T1]]> High pressure filtration stage <![CDATA[P3→T2]]> Pulse high pressure filtration stage <![CDATA[P3]]>

[0205] Example 7

[0206] The present application relates to a waste grain drying process. The contents repeated in the above embodiments are omitted. As long as there is no contradiction, the following technical features are applicable to the above embodiments, and vice versa.

[0207] The steps of S1 include:

[0208] S1-1 confirms the first threshold a and constant k1 of the current batch of samples based on the empirical table, and measures the moisture content b of the original waste;

[0209] S1-2: Determine at least three sampling points of the original dregs, weigh the total mass of the original dregs at the sampling points within the determined range and the mass of the agglomerated part after screening, and obtain the parameter A2 representing the agglomeration rate of the original dregs based on the following formula:

[0210]

[0211] S1-3 obtains the second water content M2 based on the following formula (2):

[0212] M2=b-k2×(a-A2) (2),

[0213] b represents the water content of the original waste; k2 represents a constant; A2 represents a parameter characterizing the agglomeration rate that is lower than a preset first threshold; a represents the first threshold;

[0214] S1-4 When the parameter A2 of the original waste grains provided in batches is lower than the preset first threshold value a of the relevant parameters used to characterize the agglomeration rate, the original waste grains with the parameter A2 lower than the preset first threshold value a are mechanically filtered to a second moisture content M2 in a solid-liquid separation manner.

[0215] According to a preferred embodiment, in the processing step S1, based on the gradually increasing pressure provided, the original waste grains provided in batches and having a parameter A2 lower than a preset first threshold a of the relevant parameter for characterizing the agglomeration rate are continuously mechanically filtered in a solid-liquid separation manner.

[0216] According to a preferred embodiment, as shown in Table 2, Figure 2As shown, the steps of mechanical filtration of the original waste with parameter A2 lower than the preset first threshold a include S1-4-1 pre-pressure filtration stage, S1-4-2 incremental medium-pressure filtration stage and S1-4-3 incremental high-pressure filtration stage.

[0217] Preferably, S1-4-1 pre-pressure filtration stage: the mechanical module provides initial filtration for the original waste at a set first pressure filtration pressure value.

[0218] Preferably, S1-4-2 is the incremental medium pressure filtration stage: the mechanical module filters the waste at a first pressure increase rate from a first filtration pressure value until a second filtration pressure value is reached.

[0219] Preferably, S1-4-3 is the incremental high-pressure filtration stage: the mechanical module filters the waste slag at a second pressure increase rate from the second filtration pressure value until a third filtration pressure value is reached.

[0220] Preferably, the first pressure increase rate is greater than the second pressure increase rate. Preferably, the first filter press pressure value is selected from 0.1 to 0.5 MPa. The second filter press pressure value is selected from 0.5 to 1.0 MPa. The third filter press pressure value is selected from 0.5 to 1.5 MPa.

[0221] The purpose of the pre-pressure filtration stage is to initially discharge the free water in the waste and form a preliminary filter cake structure. The waste is evenly distributed on the filter cloth (or filter frame) through filtration under low pressure. The filtration in the incremental medium pressure filtration stage is used to further discharge water, increase the density of the filter cake, and reduce the moisture content in the filter cake. The filter cake is shaped at a second filtration pressure value higher than the first filtration pressure value in this stage. The filtration in the incremental high pressure filtration stage is used to maximize the discharge of water to form a stable and dry filter cake. In this process, the second pressure increase rate should be less than the first pressure increase rate to avoid filter cake rupture or filter cloth (filter frame) clogging. The operation of slowly increasing pressure to squeeze the waste can provide a stable detection environment for detecting the moisture content of the waste. After the moisture content of the waste is less than the second moisture content, the mechanical module can directly reduce the pressure value to 0 to unload the filter cake.

[0222] Preferably, the operation procedure of the waste drying system is as follows:

[0223] Input: first threshold a, constant k2, water content b of original waste;

[0224] The sampling volume of each sample point after random sampling is calculated using the following formula:

[0225]

[0226] rand(a, b) means generating a random number in the interval [a, b]. iis the mass of the i-th sampling point, the total volume of the original waste is M, and the number of sampling points to be selected is n (n≥3),

[0227] According to the random mass range generated by formula (4), samples m1 (i.e., the above m i ), and weigh the mass m2 of the agglomerated part after screening these samples;

[0228] Calculate the average agglomeration rate A avg :

[0229]

[0230] Calculate the second moisture content M2:

[0231] M2=b-k2×(aA avg ) (9);

[0232] The control mechanical module performs the following operations:

[0233] Continuously filter at a first filter pressure value P1 for a preset time length;

[0234] The mechanical filter press pressure is regulated by the following formula until the second filter press pressure value P2 is reached:

[0235] P2=P1+r1×t (10),

[0236] r1 is the first pressure growth rate, t is the duration;

[0237] The mechanical filter press pressure is regulated by the following formula until the third filter press pressure value P3 is reached:

[0238] P3=P2+r2×t (11),

[0239] r2 is the first pressure increase rate, t is the duration, r1>r2.

[0240] Table 2

[0241] Filter pressing stage Pressure conditions (pressure-filtration rate) Pre-pressure filtration stage <![CDATA[P1(t)]]> Incremental medium pressure filtration stage <![CDATA[P1→r1→P2]]> Incremental high pressure filtration stage <![CDATA[P2→r2→P3]]>

[0242] Example 8

[0243] This embodiment proposes a dehydration treatment method and system based on the waste dregs agglomeration rate. The contents repeated in the previous embodiment are omitted. As long as there is no contradiction, the following technical features are applicable to the previous embodiment, and vice versa.

[0244] The drying module used in the present application to provide heating or constant temperature dehydration for the spent grains is, for example, a paddle dehydration device or a cyclone dehydration device.

[0245] According to a preferred embodiment, Figure 3 As shown, for the lost grains that have been filtered to a first moisture content, at a first temperature corresponding to the relevant parameters characterizing the agglomeration rate, the lost grains with the first moisture content are dehydrated at a constant temperature until a second moisture content is reached in a manner of removing water from the lost grains and gas that affects the agglomeration rate, and then the lost grains that have been dehydrated at a constant temperature to the second moisture content are dehydrated by increasing the temperature.

[0246] According to a preferred embodiment, Figure 3 As shown, for the waste slag filtered to the second moisture content, the waste slag with the second moisture content is heated and dehydrated at the first temperature corresponding to the parameter related to the agglomeration rate. The heating and dehydration process starts from the first temperature corresponding to the parameter related to the agglomeration rate as the starting point, until the second temperature is lower than the critical point of the waste slag combustion, and the second temperature is maintained until the waste slag reaches its third moisture content.

[0247] Preferably, the drying module is configured to: based on an instruction indicating a first temperature transmitted by the control unit, stir the waste grains having a first moisture content while maintaining a first temperature; Figure 3 As shown, when the water content of the wasted dregs is reduced to the second water content, the temperature is continuously raised from the first temperature to the second temperature lower than the critical point of combustion of the wasted dregs, and the second temperature lower than the critical point of combustion of the wasted dregs is continuously maintained before the water content of the wasted dregs is reduced to the third water content, or before the first temperature is raised to the second temperature lower than the critical point of combustion of the wasted dregs, the water content of the wasted dregs is reduced to the third water content and heating is stopped.

[0248] Preferably, the drying module is configured as follows: based on an instruction indicating the first temperature transmitted by the control unit, for the second moisture content of the lost grits, the temperature is continuously raised from the first temperature to a second temperature lower than the critical point of combustion of the lost grits, and the second temperature is continuously maintained lower than the critical point of combustion of the lost grits before the moisture content of the lost grits is reduced to a third moisture content, or the moisture content of the lost grits is reduced to the third moisture content before the first temperature is raised to the second temperature lower than the critical point of combustion of the lost grits, and heating is stopped.

[0249] Preferably, the control unit is configured to: obtain the first temperature of the waste grains for the second moisture content based on a set empirical table.

[0250] Preferably, the operation procedure of the waste drying system is as follows:

[0251]

[0252]

[0253] in: is the first temperature of the waste grains with the first moisture content; is the first temperature of the waste with the second moisture content; T 表格 It is a temperature calculation function based on an empirical table; and are the first water content and the second water content respectively; w3 is the third water content; T max is the second temperature below the critical point of spent grain combustion; T(t) is the temperature at time t.

[0254] Considering that the dehydration process is the last process in the dehydration process, the maximum temperature of the second temperature in the process cannot exceed 335°C (the critical point of combustion of dry lees). The maximum temperature of the first temperature cannot exceed 70°C (to reduce the risk of protein denaturation in the lees). When the water content of the lees drops to the preset third water content, stop heating or dehydrate the lees at a constant temperature.

[0255] Preferably, the third moisture content ranges from 5% to 18%. Preferably, the third moisture content is 5%, 8%, 10%, 15%, 16%, 17% or 18%.

[0256] Example 9

[0257] This embodiment relates to a waste dregs drying system. This embodiment also relates to a waste dregs processing system using the viscosity of the waste dregs as a filter press classification standard. The contents repeated in the previous embodiment are omitted. As long as there is no contradiction, the following technical features are applicable to the previous embodiment, and vice versa.

[0258] Since protein and cellulose are the components with the highest organic content in the waste (up to more than 60%), considering the retention of protein and / or cellulose in the actual screening process (for subsequent feed processing), the organic matter in this application is, for example, protein; protein and cellulose; protein, starch and cellulose; cellulose; starch; cellulose and starch; protein, starch, cellulose and fat.

[0259] Methods for detecting organic matter content include dry burning method (applicable to detection of various organic matter contents), near infrared spectroscopy analysis (applicable to detection with relatively high precision requirements), ultraviolet spectrophotometer method (applicable to detection of protein content alone), and enzyme method (applicable to detection of cellulose, starch or both content alone). Based on the requirements of organic matter detection settings, the first detection module includes related equipment for detecting organic matter content by dry burning method, related equipment for detecting organic matter content by near infrared spectroscopy analysis, related equipment for detecting organic matter content by ultraviolet spectrophotometer method, and / or related equipment for detecting organic matter content by enzyme method.

[0260] The threshold setting of the organic matter content can be set according to the experience table of relevant personnel. For example, the first threshold value can be set differently for the waste grains produced by different types of liquor, the waste grains produced in different seasons, or the waste grains produced by different raw materials.

[0261] According to a preferred embodiment, the mechanical module mechanically filters the original waste grains according to the process parameters of each batch in a manner that the preset first threshold is updated for each batch.

[0262] The storage component of the control unit stores the first process parameter, the second process parameter and the first threshold value. Preferably, the first process parameter characterizing the moisture content of the original lees is measured by the second detection module. The first process parameter measured by the second detection module is sent to the control unit and stored in the storage component. Preferably, the second process parameter matching the corresponding batch is input into the storage component of the control unit from the input end. More preferably, the second process parameter is a process parameter that affects the lees agglomeration rate. The first threshold value of each batch is input into the storage component of the control unit from the input end.

[0263] The control unit generates a corresponding experience table with the first process parameter, the second process parameter and the first threshold value stored in its storage component. The first threshold value is a dependent variable corresponding to the first process parameter and the second process parameter as independent variables.

[0264] When receiving the first process parameter updated corresponding to the current batch and the second process parameter updated corresponding to the current batch, the control unit updates the first threshold corresponding to the current batch by calling the experience table pre-stored in its storage module. The control unit updates the first threshold corresponding to the current batch using the first process parameter and the second process parameter that are closest to the first process parameter and the second process parameter of the current batch and exist in the experience table as reference independent variables for updating the first threshold.

[0265] The empirical table for characterizing the first threshold value of the agglomeration rate may be a table filled in by an operator based on experience, as shown in Table 3 below.

[0266] Table 3

[0267]

[0268] It should be noted that the first threshold value characterizing the agglomeration rate (for example, the agglomeration mass ratio) can be pre-stored in the control unit according to the operator's experience, and the influences that may be involved include but are not limited to the cellar type, the moisture content of the original discarded grains, the production time of the discarded grains (which can be accurate to days), the application type of Daqu, the raw materials of the wine mash, and the pH value of the original discarded grains.

[0269] The first temperature corresponding to the relevant parameter characterizing the agglomeration rate can also be obtained by relying on the empirical data table. The operator can determine the dehydration temperature according to the source of the waste dregs and the first parameter, the second parameter or the third parameter in the waste dregs, such as Table 4.

[0270] Table 4

[0271]

[0272] According to a preferred embodiment, the heated and dehydrated dregs separated from the high-fiber dregs and the organic-enriched dregs are screened in a differential separation method based on protein content to obtain the oversize material for pyrolysis and the undersize material for feed.

[0273] The screening module is, for example, an oscillating screening device or a drum screening device. According to the experimental data shown in Examples 2 to 5 in Table 5, the spent grains obtained under treatment under different conditions can be screened through 60 or 80 meshes, which does not affect the screening of crude protein.

[0274] Table 5

[0275]

[0276] In the above examples, after different filtration and heating treatments, the water content of the spent dregs is significantly reduced, and can finally be separated by a 60-mesh or 80-mesh sieve, and the screening process does not significantly affect the crude protein content. This shows that through reasonable filtration and heating treatment, not only can the water content of the spent dregs be effectively reduced, but also more efficient screening can be achieved.

[0277] In addition, the oversize used for pyrolysis is usually a high-fiber content fraction, which is more suitable for pyrolysis treatment due to its lower moisture content and higher calorific value, thereby producing high-quality pyrolysis gas and biochar.

[0278] In addition, the screened material used for feed is usually a part rich in organic matter and crude protein. The crude protein content of the slag after screening can be maintained at a high level, such as 17.6% in Example 3, which makes these screened materials more suitable as feed or feed additives, and improves the nutritional value of the feed. By implementing the above-mentioned treatment method, the water content of the slag can be effectively reduced, efficient screening can be achieved, and the crude protein content in the slag can be maintained or increased, and finally the slag can be efficiently utilized in pyrolysis and feed. This method combines the known technologies such as filter pressing, heating and screening, and has significant technical effects and practical application value.

[0279] It should be noted that the above-mentioned specific embodiments are exemplary, and those skilled in the art can come up with various solutions inspired by the disclosure of the present invention, and these solutions also belong to the disclosure scope of the present invention and fall within the protection scope of the present invention. Those skilled in the art should understand that the present invention specification and its drawings are illustrative and do not constitute a limitation of the claims. The scope of protection of the present invention is defined by the claims and their equivalents. The present invention specification contains multiple inventive concepts, such as "preferably", "according to a preferred embodiment" or "specifically", all of which indicate that the corresponding paragraph discloses an independent concept, and the applicant reserves the right to file a divisional application based on each inventive concept. Throughout the text, the features guided by "preferably" are only an optional method and should not be understood as being required. Therefore, the applicant reserves the right to abandon or delete the relevant preferred features at any time.

Claims

1. A method for drying waste grains, characterized in that: The method comprises the following steps: S1 mechanically filtering the original waste dregs provided in batches in a solid-liquid separation manner, wherein waste dregs having a first moisture content and a second moisture content having different moisture contents are provided in a manner related to the relevant parameters used to characterize the agglomeration rate, wherein the first moisture content is greater than the second moisture content; S2 dehydrates the spent grains by removing water and gas that affects the agglomeration rate, wherein: S2.1 For the waste slag filtered to a first moisture content, at a first temperature corresponding to a parameter related to the agglomeration rate, the waste slag with the first moisture content is subjected to constant temperature dehydration until a second moisture content is reached, and then the waste slag dehydrated to the second moisture content is subjected to temperature-raising dehydration, or S2.2 For the waste grains filtered to the second water content, the waste grains with the second water content are heated and dehydrated. The heating and dehydration process starts from the first temperature corresponding to the parameter characterizing the agglomeration rate as a starting point, and continues until the second temperature is lower than the critical point of the waste grain combustion, and the second temperature is maintained until the waste grain reaches the third water content; S3 screens the heated and dehydrated dregs separated from the high-fiber dregs and the organic-enriched dregs in a differential separation method based on protein content to obtain the oversize material for pyrolysis and the undersize material for feed.

2. The method for drying the waste grains according to claim 1, characterized in that: In the step S1, the mechanical module for mechanically filtering and dehydrating the original lost grains exerts a squeezing effect on the original lost grains according to the applied pressure, and discharges part of the liquid containing free water and capillary water through the pores of the solid matter in a manner that the solid matter in the original lost grains is retained and the solid matter is transferred to a drying module for removing moisture in the solid particles and gas that affects the agglomeration rate.

3. The method for drying the waste grains according to claim 2, characterized in that: In the step S1, the mechanical module mechanically filters the original waste grains in a manner of a preset first threshold value of the relevant parameters for characterizing the agglomeration rate updated for each batch and according to the process parameters affecting the agglomeration rate for each batch.

4. The method for drying the waste grains according to claim 2, characterized in that: In the S2 step, the drying module provides heat to the waste slugs which are transported after filtration by the mechanical module and are at a first moisture content or a second moisture content due to the capillary water and bound water present therein, and dehydrates the waste slugs with a first moisture content in a manner of reducing the agglomeration rate of the waste slugs by removing the capillary water and bound water distributed in the solid matter in the waste slugs.

5. The method for drying the waste grains according to claim 1, characterized in that: In step S1, the second detection module for detecting the moisture content of the original lost grains collects the moisture content of the original lost grains and transmits it to the control unit, wherein, through formula (1), the control unit for generating the corresponding lost grains drying treatment method calculates the first moisture content M1 of the original lost grains for which the relevant parameter characterizing the agglomeration rate exceeds or equals to the preset first threshold value based on the moisture content transmitted by the second detection module: M1=b-k1×(A1-a) (1), b represents the water content of the original waste; k1 represents a constant; a represents a first threshold; A1 represents a related parameter that exceeds or is equal to the preset first threshold a.

6. The method for drying the waste grains according to claim 1, characterized in that: In the step S1, the second detection module for detecting the moisture content of the original waste dregs collects the moisture content of the original waste dregs and transmits it to the control unit, wherein the control unit for generating the corresponding waste dregs drying treatment method calculates the second moisture content M2 of the original waste dregs whose relevant parameters characterizing the agglomeration rate are lower than the preset first threshold value based on the moisture content transmitted by the second detection module through formula (2): M2=b-k2×(a-A2) (2), b represents the water content of the original waste; k2 represents a constant; a represents a first threshold; and A2 represents a related parameter that is lower than the preset first threshold a.

7. The method for drying the waste grains according to claim 5, characterized in that: At least one parameter for characterizing the agglomeration rate is set as a first parameter representing the organic matter content, wherein, When the first parameter exceeds or is equal to the preset first threshold, the mechanical module for mechanically pressing and dehydrating the original waste dregs presses the original waste dregs whose first parameter exceeds or is equal to the preset first threshold to a first moisture content calculated by the control unit according to formula (1).

8. The method for drying the waste grains according to claim 6, characterized in that: The at least one parameter for characterizing the agglomeration rate is set as a first parameter representing the organic matter content, wherein, When the first parameter is lower than a preset first threshold, the mechanical module presses the original waste grains whose first parameter is lower than the preset first threshold to a second moisture content calculated by the control unit according to formula (2).

9. The method for drying the waste grains according to claim 1, characterized in that: The relevant parameters for characterizing the agglomeration rate include a second parameter calculated from the mass of the agglomerated portion and the total sample mass. The second parameter is calculated by formula (3):

10. A system for drying waste grains, characterized in that: The system comprises a mechanical module for mechanically filtering and dehydrating the original spent grains, a first detection module for detecting at least one parameter characterizing the agglomeration rate in the original spent grains, a drying module for heating the spent grains at a constant temperature or at a rising temperature, and a screening module for screening the dried spent grains, wherein the system is configured as follows: The mechanical module mechanically filters the raw waste provided in batches in a solid-liquid separation manner, wherein: When at least one parameter of the original waste grains detected by the first detection module for characterizing the agglomeration rate exceeds or is equal to a preset first threshold value of the relevant parameter for characterizing the agglomeration rate, the mechanical module presses the original waste grains whose relevant parameters exceed or are equal to the preset first threshold value to a first moisture content, When at least one parameter used to characterize the agglomeration rate of the original waste grains detected by the first detection module is lower than a preset first threshold value of the relevant parameter used to characterize the agglomeration rate, the mechanical module presses the original waste grains whose relevant parameter is lower than the preset first threshold value to a second moisture content, wherein the first moisture content is greater than the second moisture content; The drying module dehydrates the waste grains by removing the water in the waste grains and the gas that affects the agglomeration rate, wherein: For the waste grains filtered to a first moisture content, the drying module performs constant temperature dehydration on the waste grains with the first moisture content at a first temperature corresponding to a parameter related to the agglomeration rate until the waste grains reach a second moisture content, and then performs temperature-raising dehydration on the waste grains dehydrated to the second moisture content; or For the waste grains filtered to a second moisture content, the drying module heats and dehydrates the waste grains with the second moisture content at a first temperature corresponding to a parameter related to the agglomeration rate; The screening module screens the heated and dehydrated dregs separated from the high-fiber dregs and the organic-enriched dregs in a differential separation method based on protein content to obtain the overscreen material for pyrolysis and the underscreen material for feed.

Images