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 winemaking, and in particular to a system and method for drying and treating spent grains. Background Art

[0002] Spent grains are a solid byproduct of solid-state liquor production. In actual production, the ratio of liquor to spent grains is 1:3-4, meaning that for every ton of liquor produced, 3-4 tons of spent grains are generated. Untreated spent grains have the characteristics of high yield, high residual organic acid esters, high acidity, susceptibility to mold, and high moisture content. Therefore, they require treatment before discharge or pyrolysis to reduce pollution to soil, water, and air.

[0003] The waste grain drying device used in the prior art generally feeds the waste grain directly into a feeder, heats it with a hot air blower, and dries it in a drying chamber. The inventors have 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 clump. Direct heating and dehydration will often be affected by temperature and result in dry surface and wet inside.

[0005] Waste grains contain rich protein components, and the pyrolysis process will produce sulfides and nitrogen oxides, and the cost of treating pyrolysis exhaust gas is high.

[0006] Furthermore, the inventors explored the energy consumption of dried grains using a single heating method, and explored the combination of multiple heating methods under the single heating condition. Taking mechanical dehydration and heating dehydration as examples, the inventors explored the effects of mechanical dehydration and heating dehydration on dried grains. 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 thermal dehydration is positively correlated with the increase in energy consumption, and the slope of the curve is low, approximately a straight line. Thermal dehydration can reduce the water content of the spent grains to below 10%. When the inventors conducted an energy consumption study by combining thermal dehydration and mechanical dehydration, they found that taking spent grains with a water content of less than 10% as the target for pyrolysis, and combining thermal 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 waste dregs, even with the same process and preset processing parameters, the residual amount of waste 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 separated undersize materials varies greatly. After long-term observation, the inventors found that the agglomeration rate of different batches of waste dregs before dehydration becomes a key factor in the dehydration and screening process, and by differentiating the feeding time and processing process of mechanical filtration and heating dehydration for waste dregs with different agglomeration rates due to composition and environment, the dehydration energy consumption is reduced, the crude protein content of the undersize material is increased, and the dispersion degree of the oversize material is increased (for improving 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 objects 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 objectives of the present invention is to provide a method and system for reducing the risk of agglomeration during the dehydration process 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] The prior art has already presented a technical solution for dehydrating winemaking waste by heating. For example, CN116809611A discloses a recycling method for white wine lees, which first performs a drying process on the waste, and then sieves the dried white wine lees into light waste and heavy residue, then packs the heavy residue and stores it for other uses, performs anoxic pyrolysis on the light waste and recovers solid residue, gas-liquid products and heat energy respectively, and finally purifies the gas-liquid products and discharges them to complete the recycling of the white wine lees. However, this technical solution only involves a heating and dehydration method, and the reduction in the water content of the waste under heating and dehydration is positively correlated with the increase in energy consumption, which means that a large amount of energy needs to be consumed during the dehydration process, resulting in increased costs. Traditional heating and dehydration methods, such as the 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; and gradually reducing the moisture content of the waste dregs using at least one, preferably two, or more preferably multi-stage drying system. Here, energy consumption and dehydration efficiency are optimized by precisely controlling the drying temperature and humidity. Here, when the waste dregs provided have a first moisture content, the operating temperature of the dehydration device (paddle type) is set to a first temperature, and dehydration is performed at a constant temperature of the first temperature in the dehydration device (paddle type) until the second moisture content is reached, and then the temperature is increased 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 performed at a temperature before the critical point of combustion until the third moisture content is reached. Here, when the operating temperature of the dehydration equipment (paddle type) is set to the first temperature based on the moisture content of the pretreated waste, relevant parameters characterizing the agglomeration rate are also considered, especially the organic matter content (first parameter) previously measured based on 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 an adsorbent to capture harmful gases during the pyrolysis process; and 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 treatment method and system for reducing the risk of agglomeration during the dehydration process of the spent grains, comprising the following steps: using stirring drying technology to maintain a uniform distribution of the spent grains; and using vibrating screening equipment to further prevent agglomeration.

[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 a waste dregs, which may include the following steps: S1 mechanically filtering the original waste dregs provided in batches in a solid-liquid separation manner, wherein a waste dregs having a first moisture content and a waste dregs having a second moisture content different from each other are provided in a manner related to the relevant parameters for characterizing the agglomeration rate, wherein the first moisture content is greater than the second moisture content; S2 dehydrating the waste dregs in a manner of removing moisture and gas affecting the agglomeration rate from the waste dregs, wherein S2.1 dehydrates the waste dregs having the first moisture content at a first temperature corresponding to the relevant parameters for characterizing the agglomeration rate. Constant temperature dehydration is performed until a second moisture content is reached, and then the waste grits that have been constant temperature dehydrated to the second moisture content are subjected to temperature dehydration, or S2.2 the waste grits that have been filtered to the second moisture content are subjected to temperature dehydration, wherein the temperature dehydration is started from a first temperature corresponding to the relevant parameters characterizing the agglomeration rate, and the temperature is increased until a second temperature lower than the critical point of combustion of the waste grits is reached and the second temperature is maintained until the waste grits reach their third moisture content; S3 the waste grits that have been heated and dehydrated after separation of high fiber waste grits and organic matter enriched waste grits are screened in a manner based on differential separation of protein content to obtain the oversize material for pyrolysis and the 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] The original discarded dregs in this application refer to the untreated dregs remaining after the completion of winemaking and no longer used for fermentation.

[0026] Unlike the prior art, the present invention can simultaneously use mechanical dehydration and heating dehydration to dehydrate the spent grains, wherein corresponding dehydration methods are set according to the 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 in 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 overall energy consumption.

[0027] Preferably, the mechanical filtration comprises the following steps: mechanically filtering the original slop with a moisture content of 57-62% by solid-liquid separation at a filtration pressure of 0.8-1.2 MPa to reduce the moisture content of the slop to 35-40%, discarding the filtrate, and collecting the slop. Thermal dehydration comprises the following steps: dehydrating the slop to remove moisture and gases that affect the agglomeration rate until the moisture content is reduced to 8-10%. Screening the slop with a moisture content reduced to 8-10% by differential separation based on protein content to obtain an oversize for pyrolysis and an undersize for enrichment of organic matter.

[0028] More preferably, the original lees, with a moisture content of 57.6%, is mechanically filtered using a solid-liquid separation method at a pressure of 1.2 MPa to reduce the moisture content to 35.9%. The filtrate is discarded and the lees are collected. The lees are then dehydrated by heating at 180°C for 15 minutes until the moisture content is reduced to 8.1%. The lees, having a moisture content of 8.1%, are sieved through an 80-mesh screen to obtain an oversize fraction for pyrolysis and an undersize fraction having a crude protein content of not less than 7%.

[0029] Beneficial effects of this technical solution:

[0030] 1. The inventors investigated the pyrolysis of spent grains with a moisture content of up to 65%, and through experiments combining multiple dehydration methods, they identified a low-energy, high-efficiency drying system that can simultaneously solve the problems of uneven pyrolysis and gas pollution.

[0031] Based on the energy consumption control experiment provided in Example 1, it can be seen 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 significantly reduce 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 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 thermal dehydration, found that taking spent grains with a moisture content of less than 10% as the target for pyrolysis, combining mechanical dehydration and thermal 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 for spent grain dehydration operations.

[0033] 2. Related research results show that the crude fiber content of the solid after the dried lees is more than 30%. The crude fiber content mainly comes from the rice husk component added during fermentation. This part can produce pyrolysis gas through pyrolysis, which can be burned to provide energy for production. However, the crude protein content of the solid after the dried lees is more than 7% (see Examples 2 to 5). Direct pyrolysis will cause a large amount of sulfide and nitrogen oxides to be produced during the pyrolysis and combustion process. Therefore, the current lees treatment 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 waste grain treatment process lead to increased waste grain treatment costs.

[0035] Taking into account that when the spent grains are directly pyrolyzed, they will produce high levels of sulfides and nitrogen oxides due to the rich protein components. The spent grains processing process of this application is equipped with a screening step. By screening, the crude fiber and low protein content components (oversize) in the spent grains are screened out for subsequent pyrolysis, while the high protein and low fiber part (undersize) can be used in other fields. This application will screen the spent grains after dehydration and drying. The screened upper layer of spent grains is mainly crude fiber components. The protein content of this type of crude fiber component is extremely low. This part of the spent grains is burned to provide energy for production. The tail gas treatment is easier, there are fewer pollutants, and the cost is lower.

[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 waste, the dispersion degree of the screen material produced by the linear mechanical filter press-heated filter press process was unstable, and the screen material produced by some of the treated waste still had the problem of inefficient pyrolysis. At the same time, the organic matter content of the screen material produced (this application takes crude protein as an example) was relatively large, making it impossible to control the quality of the treated waste when used as a pyrolysis material and feed additive. Waste with a high agglomeration rate has a high viscosity. After pressure compression, it is not only difficult to be evenly stirred by a stirring device, but it may also further increase the waste agglomeration rate in the process of reducing the water content. At the same time, waste with a high agglomeration rate is more likely to have waste clumps with a diameter exceeding a certain range that cannot be broken up. Such waste clumps will form solid clumps with a soft inside and a dry outside during the dehydration process (which cannot be broken up by simple shearing or stirring), which increases the difficulty of screening.

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

[0038] The present application enables the waste 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 waste grains during the heating process, making it easier to deagglomerate, thereby improving the efficiency of stirring the waste grains. On the other hand, the high heat capacity of water can provide more uniform heat conduction for the waste grains during the heating process, avoiding local overheating of the waste grains and uneven dehydration uniformity inside and outside the grains.

[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 mechanical module preferably includes a double-screw filter press, a servo hydraulic system, an online viscometer, a pre-crushing blade group, and a filter cloth self-cleaning device. 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 first detection module preferably includes a rotary viscosity sensor, a laser particle size analyzer, and a near-infrared moisture meter to obtain the viscosity, water content, particle distribution and other agglomeration rate characterizing parameters of the waste dregs. The waste dregs drying treatment system includes a drying module for constant temperature heating or temperature-raising heating of the waste dregs. The drying module preferably includes a paddle dryer, a hot air circulation system, a centrifugal crusher, and a dew point sensor. The waste dregs drying treatment system includes a screening module for screening the dried waste dregs. The screening module can separate high-fiber waste dregs (overscreen) and organic matter-enriched waste dregs (underscreen) based on differences in protein content. The screening module preferably includes a multi-layer vibrating screen, a pneumatic conveying system, a photoelectric separator, and an ultra-granular crusher.

[0040] According to a preferred embodiment, the specific operation process of the lees drying treatment system is as follows: a first detection module detects the agglomeration rate parameter of the original lees. Based on the measured agglomeration rate parameter, the mechanical module performs filter pressing on the original lees in batches. Furthermore, the drying module heats the lees treated by the mechanical module at a constant temperature or at an elevated temperature to obtain dried lees. The dried lees are then sorted by a screening module to ultimately obtain the target substance. The screening module preferably dynamically adjusts the mesh size and sorting threshold based on the protein content test results of the lees.

[0041] Preferably, the mechanical module and the drying module are connected by a high-temperature resistant screw conveyor.

[0042] Preferably, a buffer hopper is provided between the drying module and the screening module.

[0043] According to a preferred embodiment, the waste grain drying system is configured such that a mechanical module mechanically filters batches of raw waste grains to separate solids and liquids. When a first detection module detects that at least one parameter characterizing the agglomeration rate of the raw waste grains exceeds or equals a preset first threshold value for the parameter characterizing the agglomeration rate, the mechanical module filters the raw waste grains, whose parameter exceeds or equals the preset first threshold value, to a first moisture content.

[0044] Specifically, the first detection module transmits the agglomeration rate parameter to the mechanical module in real time to control the target moisture content for filter pressing. The drying module automatically selects either a constant temperature or elevated temperature mode based on the moisture content data output by the mechanical module. The dried grains processed by the drying module are then transferred to the screening module, which sorts the grains based on their protein content.

[0045] According to a preferred embodiment, the waste grains drying treatment system is configured as follows: 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 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.

[0046] 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 that removes moisture and gas that affects the agglomeration rate in the wasted grains, wherein, for the wasted grains that are 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 are dehydrated to the second moisture content; or for the wasted grains that are 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.

[0047] According to a preferred embodiment, the lees drying treatment system is configured as follows: the screening module screens the heated and dehydrated lees separated from the high-fiber lees and the organic-enriched lees in a differential separation method based on protein content to obtain the oversize material for pyrolysis and the undersize material for feed.

[0048] Beneficial effects of this technical solution:

[0049] The present application adjusts the pressure regulation process in the filtration process and performs differentiated filtration pressure treatment on the waste grains with different agglomeration rates, so that the waste grains can enter the dehydration process based on transpiration with different water contents, so that the waste grains with high agglomeration rates can retain more moisture and higher conductivity. During the stirring process, the waste grains with high agglomeration rates are more easily broken up due to the influence of high water content.

[0050] The agglomeration rate not only affects the filtration 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. 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 treatment method proposed in the present application can obtain organic matter aggregated particles with a crude protein content of more than 7% without crude fiber.

[0051] 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 according to formula (1):

[0052] M1=b-k1×(A1-a) (1),

[0053] b represents the moisture 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; and a represents the first threshold.

[0054] According to a preferred embodiment, in the processing step S1, the first water content M1 can be calculated by formula (1).

[0055] 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 second moisture content M2 according to formula (2):

[0056] M2=b-k2×(a-A2) (2),

[0057] b represents the moisture content of the original waste; k2 represents a constant; A2 represents a related parameter that is lower than a preset first threshold a; and a represents the first threshold.

[0058] According to a preferred embodiment, in the processing step S1, the second water content M2 can be calculated by formula (2).

[0059] Beneficial effects of this technical solution:

[0060] This application introduces the relationship between the agglomeration rate and the preset threshold value, allowing the operator to 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 waste grains, and meeting the quality control of the waste grains in different batches for different application purposes or different factory states.

[0061] K1 in formula (1) and k2 in formula (2) both represent constants used to optimize the calculation of moisture content. Workers can determine suitable constant values ​​based on different processing requirements or relevant experimental data.

[0062] The preset first threshold a is set manually based on empirical tables. Moisture content is a key factor affecting the agglomeration rate of raw lees. Different batches of raw lees also have different agglomeration rates due to factors such as the cellar, fermentation season, and raw materials. Based on this, the a value in formulas (1) and (2) can be set using empirical tables.

[0063] According to a preferred embodiment, in step S1, a mechanical module for mechanically pressing and dehydrating the raw slops squeezes the raw slops by applying pressure, and partially discharges the liquid, including free water and capillary water, through the pores of the solid matter, thereby retaining the solid matter in the raw slops and transferring the solid matter to a drying module for removing moisture from the solid particles and gases that affect the agglomeration rate. This filtration method reduces slop agglomerates caused by polymerized proteins in the solid matter using free water as a medium. Preferably, the solid matter includes protein, plant fiber, microbial residues, and microbial metabolic residues.

[0064] Beneficial effects of this technical solution:

[0065] Although simple extrusion, especially the extrusion method with continuously increasing pressure, can intercept solid matter in the original waste, it also forces some gases to increase their solubility in the liquid, and even form clumps and lock a large number of bubbles and water in a large number of clumps. 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 clumps 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 clumps with free water as the medium, thereby eliminating the formation process of clumps containing water bubbles or bubbles.

[0066] The water locked in the mass exists in the form of free water, capillary water and bound water.

[0067] A liquid in the form of free water is, for example, a liquid that does not form strong interactions with solute molecules.

[0068] Capillary water is liquid trapped in pores or fibers within a material by capillary action. Due to capillary action (i.e., surface tension and adhesion), capillary water must overcome the forces between it and the solid material to be expelled. Therefore, even under increased pressure, some capillary water, where the forces between it and the solid material are greater, may remain within the solid material.

[0069] Because the solid matter in the waste grains contains a lot of fibers, when separating the liquid and solids, the liquid in the form of free water retained in the solid clumps will be separated first. Considering that the energy consumption of mechanical filter pressing is much lower than that of heated filter pressing, mechanical filter pressing prioritizes squeezing the liquid in the form of free water in the waste grains through the pores in the solid matter (especially the clumps of solid matter). At the same time, during the process of applying pressure, some liquid in the form of capillary water will also be squeezed out.

[0070] Spent grains contain a high percentage of water (usually between 60% and 80%) and also include unfermented starch, protein, cellulose, fat, and microbial cells. As the water content of the grains decreases, the difference in agglomeration rate increases, and the unfermented starch, protein, cellulose, and other components in the grains form a water-absorbing network, hindering the dehydration of the grains. At the same time, as water is lost, the clumps or lumps in the grains become increasingly compact and difficult to break apart. (With the removal of water, the distance between solid particles in the clumps or lumps decreases, and for example, unfermented starch, protein, and cellulose become more closely connected. The removal of water reduces the lubrication between the particles, increasing the friction and bonding between the solid particles. The dehydration process may also involve chemical changes that increase the density of the grains, including protein denaturation and starch gelatinization.)

[0071] 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 it. Liquid in the form of free water can be discharged through simple mechanical filter pressing. When the pressure of the mechanical filter pressing 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 polymerization 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 will be reduced, so that more proteins can be 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 effect on grit agglomeration, and also makes it easier to break up the grits that become filter cakes due to external squeezing during the stirring process.

[0072] According to a preferred embodiment, the drying module provides heat to the waste grits which are transferred 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 by removing the capillary water and bound water distributed in the solid matter in the waste grits in a manner that reduces the agglomeration rate of the waste grits.

[0073] Beneficial effects of this technical solution:

[0074] 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 critical value of combustion or even higher temperatures are reached, and may even form a hydration reaction related to protein modification. Therefore, according to the present invention, the waste slag at the first water content after the filtration process is stirred at a high speed before it is 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 are mechanically dispersed by mutual collision during the feeding stage, avoiding the half-barrel effect caused by the downward sedimentation of the agglomerates under the action of gravity, that is, the high-water content agglomerates under pressure will accumulate at the bottom and continue to accumulate in the lower half stirring zone at high temperature, together forming a "shell" formed by the waste slag facing the stirring mechanism, which 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 rate or the feeding rate change rate is pre-set according to both the stirring speed and the moisture content (first or second).

[0075] At the same time, during the heating process, a large amount of liquid in the form of bound water in the agglomerate will also come into contact with 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. Liquids in the form of bound water are, for example, liquids that form strong interactions with solute molecules, ions or other components. Such liquids are tightly bound to solutes through hydrogen bonds, ion-dipole interactions or other chemical bonds, and this binding usually changes the physical and chemical properties of water. For example: in the waste dregs, the liquid can form hydrogen bonds with polar groups on the surface of proteins (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 in a way that destroys the chemical bonds formed between the liquid in the form of bound water and the proteins in the waste dregs, and based on energy accumulation, evaporates 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.

[0076] This technical solution provides high temperature conditions, which affect the solubility and viscoelasticity of proteins by deforming the proteins and breaking the chemical bonds, and increase the possibility of deformed proteins aggregating in the form of large particles (rather than a network), 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.

[0077] 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 parameter related to the agglomeration rate updated for each batch and according to the process parameters affecting the agglomeration rate for each batch.

[0078] Preferably, process parameters affecting the clumping rate include, but are not limited to, pit type, moisture content of the original spent grains, spent grains production time (accurate to the day), type of Daqu application, raw materials for the fermented mash, and pH value of the original spent grains. For details on adjusting the first threshold value based on process parameters, see the Examples.

[0079] Beneficial effects of this technical solution:

[0080] 1. Parameters for each batch of spent grains are individually configured for each season. These parameters are recorded in association with the corresponding cellar number. The resulting parameters, used to characterize the clumping rate, are correlated with spent grains quality and also provide a useful indicator of fermentation progress. These parameters, stored in association with the cellar number, can be used to refine the timing of adding materials and opening the cellars over many years of continuous production.

[0081] 2. By collecting and analyzing process parameter data related to agglomeration rate, a more accurate data model can be established, reducing manual intervention in setting the first threshold for different batches of spent grains. By using the process parameters influencing the agglomeration rate as independent variables and the dependent variables used to characterize the first threshold for the parameters related to the agglomeration rate as the dependent variables, the selection of the first threshold for each batch is more targeted, resulting in a closer correlation between the setting of the first threshold and the agglomeration rate it represents. This allows dynamic adjustment of process parameters to reduce the agglomeration rate during the spent grains processing while maintaining the consistency and stability of the quality of the processed spent grains (e.g., crude protein content).

[0082] 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):

[0083]

[0084] Beneficial effects of this technical solution:

[0085] Using the mass of the agglomerated portion and the total sample mass as evaluation parameters simplifies the acquisition of parameters related to the agglomeration rate, making this technical solution more suitable for factory or workshop operations. Compared to more complex chemical analysis methods, parameters acquired through visual inspection, image acquisition, or sieving and weighing reduce the complexity of obtaining the second parameter and increase the measurement efficiency of the second parameter.

[0086] According to a preferred embodiment, in processing step S1, the relevant parameter characterizing the clumping rate may be organic matter content. The first detection module is configured as a device related to organic matter content detection. The first threshold may be set to a numerical value of the organic matter content. Preferably, the first threshold is set between 5% and 50% by mass. More preferably, the first threshold is set to 20% by mass.

[0087] According to a preferred embodiment, at least one parameter for characterizing the agglomeration 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).

[0088] Preferably, the first detection module is configured to detect the organic matter content of the original waste, wherein, when the organic matter content detected by the first detection module exceeds or is equal to a first threshold value of the preset organic matter content, the mechanical module presses the original waste with an organic matter content exceeding or equal to the first threshold value of the preset organic matter content to a mechanical filtration 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 first threshold value of the preset organic matter content, the mechanical module presses the original waste with an organic matter content lower than the first threshold value of the preset organic matter content to a mechanical filtration to a second water content calculated by the control unit according to formula (2).

[0089] Beneficial effects of this technical solution:

[0090] Factors affecting the clumping rate include:

[0091] (1) Moisture content: Higher moisture content usually increases the viscosity and agglomeration tendency of the waste grains, while lowering the moisture content helps to reduce the amount of waste grains agglomeration.

[0092] (2) Organic matter content: Protein polymerization forms 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.

[0093] (3) Pressure during mechanical filtration: The continuous pressure exerted on the waste by the filter press dehydration equipment will lead to an increase in the waste agglomeration rate.

[0094] Considering that water is lost during the dehydration process and the proportion of free water decreases, the organic matter content that persists in the spent grains as a relevant parameter for assessing the agglomeration rate can increase the stability of the assessment results. Furthermore, because the organic matter content is highly accurate (it requires high-precision instrumentation), the agglomeration rate it represents is also highly accurate.

[0095] According to a preferred embodiment, in processing step S1, the relevant parameter characterizing the clumping rate can be a third parameter represented by a pressure value. Preferably, the first detection module is configured as a stirring pressure rod, and the pressure value (i.e., the third parameter) displayed by the stirring pressure rod during the stirring process of the waste grains is used to characterize the clumping rate of the waste grains. Preferably, the first threshold can be set as a pressure parameter. Preferably, the first threshold is set between 50 and 70 mPa·s. More preferably, the first threshold is set to 60 mPa·s.

[0096] According to a preferred embodiment, in step S2, the dehydration process includes the following steps: using the reduction of the water content of the spent grains to a third water content suitable for use as dry feed as a criterion for stopping dehydration, and performing a dehydration process from a first temperature to a preset maximum temperature on the spent grains that have been filtered to the first water content and whose water content has been reduced to the second water content, or on the spent grains that have been filtered to the second water content. According to the treatment methods described in Examples 2 to 5, spent grains with a water content of less than 20% after final dehydration can be screened to obtain a screened product having a crude protein content of not less than 7%.

[0097] In the processing step S1 , the original waste slop 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 is mechanically filtered with a gradient pressure change.

[0098] Beneficial effects of this technical solution:

[0099] Unlike the prior art, the present invention is able to evaluate the agglomeration rate of the original dregs according to the relevant parameters detected by the first detection module, and dynamically adjust the filtration 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 the dregs agglomerating or lumping during the filtration dehydration process. Specifically, in the traditional filtration 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 filtration process. If a unified filtration parameter is used to treat dregs with different agglomeration rates, the dregs with a larger agglomeration rate will be more likely to agglomerate or lump. This agglomeration or lumping will not only affect the subsequent drying effect, but may also cause the dried dregs feed to have a block or lump structure with increased firmness and hardness, thereby affecting its quality and applicability as a feed.

[0100] Compared to gradient filter pressing, staged filter pressing can also reduce energy consumption and minimize mechanical wear and tear. While gradient filter pressing requires continuous pressure buildup by overcoming the flow resistance of the waste, staged filter pressing maintains constant pressure throughout each stage. Therefore, equipment operating in staged filter pressing does not need to be constantly in the state of boosting and changing pressure, which reduces equipment wear and tear and energy consumption.

[0101] According to a preferred embodiment, in the processing step S1, based on the gradually increasing pressure provided, the original waste slop provided in batches is continuously mechanically filtered in a solid-liquid separation manner and at least one parameter characterizing the agglomeration rate is lower than a preset first threshold value of the relevant parameter characterizing the agglomeration rate.

[0102] Beneficial effects of this technical solution:

[0103] Considering that the risk of increased clumping after moisture content decreases for waste with a low clumping rate is relatively low, a gradual filter pressing procedure is used. During the gradual filter pressing process, the pressure gradually increases, which helps to drain the moisture from the waste more evenly. However, due to the gradual increase in pressure, the structure of the waste cake after filtration may become more uniform and the density may be higher. Therefore, for waste with a relatively low clumping rate, considering that clumping or agglomeration generated during the mechanical filter pressing process is easily broken up in the drying module or agitator, the filter press is set to a gradual filter pressing procedure to increase waste drainage efficiency and reduce energy consumption.

[0104] According to a preferred embodiment, in step S3, the crude protein content of 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%.

[0105] According to a preferred embodiment, the first moisture content ranges from 40% to 50%. Preferably, the first moisture content is 50%, 45% or 40%.

[0106] According to a preferred embodiment, the second moisture content ranges from 30% to 40%, preferably, the second moisture content is 30%, 40% or 35%.

[0107] Preferably, the mechanical module is configured as a plate-and-frame filter press. The specific operating steps for mechanically filtering the raw waste grains provided in batches to separate solids and liquids are, for example, as follows: the plate-and-frame filter press filters waste grains having a moisture content of 57-62% at a pressure of 0.8-1.2 MPa, reducing the moisture content of the waste grains to 35-40%, discarding the filtrate, and collecting the waste grain filter cake.

[0108] Preferably, the drying module includes a paddle dryer. The drying module dehydrates the spent grains by removing moisture and gases that affect agglomeration. Specifically, the steps include: transferring the spent grain filter cake to the paddle dryer for heating and dehydration until the spent grains have a moisture content of 8-10%; sieving the spent grains, which have a moisture content of 8-10%, to obtain an oversize fraction for pyrolysis and an undersize fraction enriched with organic matter.

[0109] More preferably, a plate and frame filter press is used to filter the 57.6% water content of the waste lees at a pressure of 1.2 MPa until the water content reaches 35.9%. The filtrate is discarded and the waste lees filter cake is collected. The filtrate is then transferred to a paddle dryer and heated at 180°C for 15 minutes to dehydrate the lees to a water content of 8.1%. The screening module then screens the lees until the water content is reduced to 8.1%.

[0110] 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.

[0111] According to a preferred embodiment, the mesh size of the sieve used for screening is 60-80 mesh. Preferably, the mesh size is 60 mesh. Preferably, the mesh size is 70 mesh. Preferably, the mesh size is 80 mesh.

[0112] According to a preferred embodiment, the filter press pressure ranges from 1 to 1.2 MPa. Preferably, the filter press pressure is 1 MPa. Preferably, the filter press pressure is 1.1 MPa. Preferably, the filter press pressure is 1.2 MPa.

[0113] 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.

[0114] According to a preferred embodiment, the heating time of the paddle dryer is in the range of 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.

[0115] 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.

[0116] 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.

[0117] 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.

[0118] 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

[0119] Figure 1 Energy consumption statistics provided by the present invention;

[0120] Figure 2 The process flow chart of step S1 provided by the present invention;

[0121] Figure 3 This is a process flow chart of step S2 provided by the present invention. DETAILED DESCRIPTION

[0122] The following is a detailed description with reference to the accompanying drawings.

[0123] In the description of the present invention, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance. "Several" means two or more, unless otherwise specifically defined. Those skilled in the art will understand the specific meanings of these terms in the present invention based on specific circumstances.

[0124] Agglomeration rate is a method used to characterize the performance of sticky mash (e.g., fermented grains) during processing. Agglomeration rate generally refers to the degree to which mash forms lumps under certain conditions. For sticky grains, the determination and control of agglomeration rate is very important. Agglomeration may affect the efficiency of solid-liquid separation, filtration rate, and product quality. Agglomeration rate refers to the proportion of grains that form lumps due to stickiness or other reasons during processing. Agglomeration rate can be expressed by measuring the proportion of agglomerated parts in grains per unit volume or mass. For example, the agglomeration rate can be calculated using the following formula:

[0125]

[0126] The clumping rate can be measured by the following methods:

[0127] 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.

[0128] 2. Manual separation method: Manually separate the sample into agglomerated and non-agglomerated parts, weigh them separately and calculate the agglomeration rate.

[0129] 3. Visual inspection or image analysis: The proportion of the agglomerated part can be roughly estimated by visual inspection of the sample or image analysis.

[0130] Example 1

[0131] When treating waste grains with high moisture content (around 60%), mechanical methods are used, and when treating waste grains with low moisture content (35% to 40%), heating methods are used.

[0132] 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 , take the filter plate size 1000mm*1000mm) as an example.

[0133] A plate and frame filter press consumes 50kJ of electricity to reduce the water content of discarded grains from 70% to 40% at a pressure of 1.0 MPa. A paddle dryer consumes 80kJ of electricity to reduce the water content of discarded grains from 70% to 40% at a heating temperature of 160°C. Based on the calculation of electricity consumption, this example calculates the energy loss for the three methods of reducing the discarded grains from 70% to 20%.

[0134] like Figure 1 As shown in the figure, in the process of gradually decreasing the moisture content of the wasted 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%).

[0135] The results show:

[0136] When mechanical dehydration is used, energy consumption increases exponentially with decreasing moisture content. Mechanical dehydration significantly reduces energy consumption when reducing the moisture content of spent grains with a moisture content of around 60% to between 35% and 40%. However, even with significantly increased mechanical intensity, it is still difficult to reduce the moisture content of spent grains to below 25% (Line A).

[0137] When using heating dehydration, the decrease in moisture content and the increase in energy consumption are positively correlated, and the slope of the curve is low, approximately a straight line. Although heating dehydration can reduce the moisture content of the spent grains to below 10%, the energy consumption required for heating dehydration gradually increases as the moisture content of the spent grains decreases (line B).

[0138] When mechanical dehydration and thermal dehydration are combined, that is, mechanical dehydration is used when treating waste grains with high moisture content (40% to 60%), and thermal dehydration is used when treating waste grains with low moisture content (35% to 40%), energy consumption is significantly reduced (line C).

[0139] Currently, the primary utilization of spent grains is as a feed additive after drying and deacidification. In recent years, pyrolysis, a method for converting high-moisture spent grains into steam and other energy sources and biochar for the brewing process, has become a research hotspot due to its rapid, clean, and large-scale processing capabilities. Numerous studies have shown that reducing the moisture content of solid waste from 80% to 30% increases the heat requirement from 70 kcal / kg to 2400 kcal / kg. According to relevant reports, when using chain furnaces to process spent grains from brewing, waste with a high moisture content cannot be fully pyrolyzed and burned in the furnace. These results indicate that the moisture content of solid waste has a significant impact on its pyrolysis.

[0140] Example 2

[0141] This embodiment provides a specific implementation method for treating the waste grains without using mechanical filtration.

[0142] The steps for waste disposal include:

[0143] (1) Collecting the solid-state liquor waste, the water content was determined to be 57.6%;

[0144] (2) The liquor waste was sent to a paddle dryer at a temperature of 180°C for 28 minutes until the water content of the waste was reduced to 9.8%.

[0145] (3) The dried waste in (2) was sieved and passed through an 80-mesh sieve. The material on the sieve was collected and the protein content was determined to be 7.0%.

[0146] Example 3

[0147] This embodiment provides a specific implementation method for treating the waste grains. Unlike the above embodiments, this embodiment does not include screening the dried waste grains.

[0148] (1) Collecting the solid-state liquor waste, the water content was determined to be 57.6%;

[0149] (2) Using a plate and frame filter press to filter the waste dregs at a pressure of 1.2 MPa, discard the filtrate, collect the waste dregs filter cake, and determine the water content to be 35.9%;

[0150] (3) The waste cake was sent to a paddle dryer at a working 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%.

[0151] Example 4

[0152] This embodiment provides a specific implementation method for waste grain processing. Unlike the above embodiments, the processing method of this embodiment optimizes the processing parameters.

[0153] (1) Collecting solid-state liquor waste, the water content was determined to be 61.8%;

[0154] (2) Using a plate and frame filter press to filter the waste dregs at a pressure of 1 MPa, discard the filtrate, collect the waste dregs filter cake, and determine the water content to be 36.8%;

[0155] (3) The waste cake was sent to a paddle dryer at a temperature of 160°C for 15 minutes. The moisture content of the waste cake was reduced to 9.8%, and the protein content was determined to be 16.8%.

[0156] (4) The dried waste from (3) was sieved and passed through a 60-mesh sieve. The material on the sieve was collected and the protein content was determined to be 7.2%.

[0157] Example 5

[0158] This embodiment provides a specific implementation method for waste grain processing. Unlike the above embodiments, the processing method of this embodiment optimizes the processing parameters.

[0159] (1) Collecting solid-state liquor waste, the water content was determined to be 61.8%;

[0160] (2) Using a plate and frame filter press to filter the waste dregs at a pressure of 1 MPa, discard the filtrate, collect the waste dregs filter cake, and determine the water content to be 36.8%;

[0161] (3) The waste cake was sent to a paddle dryer at 180°C for 12 minutes. The moisture content of the waste cake was reduced to 9.5%, and the protein content was determined to be 16.8%.

[0162] (4) The dried waste from (3) was sieved and passed through a 60-mesh sieve. The material on the sieve was collected and the protein content was determined to be 7.1%.

[0163] Example 6

[0164] This application relates to a drying process and system for waste waste with significant particle accumulation. Any content that overlaps with the previous embodiments is omitted. Unless otherwise specified, the following technical features apply to the previous embodiments, and vice versa.

[0165] The steps of S1 include:

[0166] 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;

[0167] S1-2 Determine at least three sampling points for the original waste, weigh the total mass of the original waste at the sampling points within the determined range and the mass of the agglomerated portion after screening, and obtain the parameter A1 of the original waste based on the following formula:

[0168]

[0169] S1-3 obtains the first water content M1 based on the following formula (1):

[0170] M1=b-k1×(A1-a) (1),

[0171] b represents the moisture 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;

[0172] S1-4 When the parameter A1 for characterizing 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 for characterizing 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.

[0173] According to a preferred embodiment, the original waste slag provided in batches and having a parameter A1 characterizing the agglomeration rate exceeding or equal to a preset first threshold value of the relevant parameter characterizing the agglomeration rate is mechanically filtered with a gradient pressure change.

[0174] According to a preferred embodiment, the steps of mechanical filtration of the original waste when the parameter A1 exceeds or is equal to the preset first threshold a include: S1-4-1 pulse pre-pressure filtration stage, S1-4-2 main pressure filtration stage, S1-4-3 high-pressure filtration stage, and S1-4-4 pulse high-pressure filtration stage.

[0175] 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.

[0176] The purpose of the pre-pressure filtration stage is to initially remove 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.

[0177] Preferably, as shown in Table 1, Figure 2As shown, S1-4-2 is the main pressure filtration stage: the mechanical module filters the waste grit in the mechanical module at a set second pressure value. More preferably, the main pressure filtration stage includes high-pressure stages with different filtration times and different pressures. For example: the S1-4-2-1 mechanical module filters the waste grit in the mechanical module at a set second pressure value in the first stage within a preset first time length; the S1-4-2-2 mechanical module filters the waste grit 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: continuous filtration at 1.0Mpa, switch to 0.5Mpa after 5 minutes, switch to 1.0Mpa for continuous filtration after 5 minutes, switch to 0.5Mpa after 5 minutes, and the above filtration process is repeated 3 times.

[0178] Preferably, S1-4-4 pulse high-pressure filtration stage: the mechanical module applies short-term pressure to the waste residue in the filter press mechanical module at least once at a set third pressure value until the water content of the waste residue in the mechanical module is less than the first water content.

[0179] The waste drying system further comprises a control unit having an input terminal and a computing capability, wherein the control unit is configured to determine a first threshold value a and a constant k1 based on an experience table inputted into the input terminal of the control unit or a selection instruction from an experience table pre-stored in the control unit.

[0180] The control unit is configured to calculate the parameter A1 representing the agglomeration rate of the current batch of waste grits based on the total mass ml of the waste grits (i.e., the total sample mass) and the mass m2 of the agglomerated waste grits (i.e., the mass of the agglomerated portion) transmitted by the first detection module using the following formula (4):

[0181]

[0182] 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:

[0183] M1=b-k1×(A1-a) (1),

[0184] b represents the moisture 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; and a represents the first threshold.

[0185] The first detection module is configured to collect the grits at manually confirmed sampling points or randomly generated sampling points, and weigh the total mass m1 of the grits and the mass m2 of the agglomerated grits respectively.

[0186] The second detection module is configured to detect the water content b in the original waste grains.

[0187] The mechanical module is configured to: when A1 is not less than a, filter the original waste to a first moisture content M1 using the following filter pressing steps:

[0188] Pulse filter press with a preset first pressure value;

[0189] Filtering at a preset second pressure value within a preset first time period;

[0190] Filtering at a preset third pressure value within a preset second time period;

[0191] 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 greater than the third pressure value.

[0192] Preferably, the operation procedure of the waste drying system is as follows:

[0193] Input: first threshold a, constant k1, moisture content b of original waste;

[0194] The following formula is used to calculate the sampling volume of each sample point after random sampling:

[0195]

[0196] rand(a, b) represents the generation of a random number in the interval [a, b], m 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).

[0197] According to the random mass range generated by formula (4), samples m1 of corresponding mass (i.e., the above m t ), and weigh the mass m2 of the agglomerated part after screening these samples;

[0198] Calculate the average agglomeration rate A avg :

[0199]

[0200] Calculate the first moisture content M1:

[0201] M1=b-k1×(A avg -a) (8);

[0202] The control mechanism module performs the following operations:

[0203] Pulse filter press with pressure P1;

[0204] During time T1, filter at pressure P2;

[0205] During time T2, filter at pressure P3;

[0206] 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.

[0207] Table 1

[0208] Filter pressing stage Filtration 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]]>

[0209] Example 7

[0210] This application relates to a waste grain drying process. Any content that overlaps with the previous embodiment is omitted. Unless otherwise specified, the following technical features are applicable to the previous embodiment, and vice versa.

[0211] The steps of S1 include:

[0212] 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;

[0213] S1-2: Determine at least three sampling points for the original waste, weigh the total mass of the original waste and the mass of the agglomerated portion after screening at the sampling points within the determined range, and obtain parameter A2 representing the agglomeration rate of the original waste based on the following formula:

[0214]

[0215] S1-3 obtains the second water content M2 based on the following formula (2):

[0216] M2=b-k2×(a-A2)(2),

[0217] b represents the moisture 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;

[0218] 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 parameter 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.

[0219] According to a preferred embodiment, in the processing step S1, based on the provided gradually increasing pressure, the original waste slop provided in batches and having a parameter A2 lower than a preset first threshold a of the relevant parameter for characterizing the agglomeration rate is continuously mechanically filtered in a solid-liquid separation manner.

[0220] 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.

[0221] 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.

[0222] Preferably, S1-4-2 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.

[0223] Preferably, S1-4-3 incremental high-pressure filtration stage: the mechanical module filters the waste at a second pressure increase rate from the second filtration pressure value until a third filtration pressure value is reached.

[0224] 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.

[0225] The purpose of the pre-pressure filtration stage is to initially remove free water from the waste, forming a preliminary filter cake structure. Low-pressure filtration is used to evenly distribute the waste onto the filter cloth (or filter frame). The filter pressing during the incremental medium-pressure filtration stage further removes water, increases the density of the filter cake, and reduces its moisture content. This stage uses a second pressure, higher than the first, to stabilize the filter cake. The incremental high-pressure filtration stage maximizes water removal to form a stable, dry filter cake. During this process, the second pressure increase rate should be slower than the first to prevent cake breakage or clogging of the filter cloth (or filter frame). This slowly increasing pressure while squeezing the waste provides a stable environment for testing the waste moisture content. Once the waste moisture content falls below the second pressure, the mechanical module reduces the pressure to zero to remove the filter cake.

[0226] Preferably, the operation procedure of the waste drying system is as follows:

[0227] Input: first threshold a, constant k2, moisture content b of the original waste;

[0228] The following formula is used to calculate the sampling volume of each sample point after random sampling:

[0229]

[0230] rand(a, b) means generating a random number in the interval [a, b], m tis 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),

[0231] According to the random mass range generated by formula (4), samples m1 of corresponding mass (i.e., the above m i ), and weigh the mass m2 of the agglomerated part after screening these samples;

[0232] Calculate the average agglomeration rate A avg :

[0233]

[0234] Calculate the second moisture content M2:

[0235] M2=b-k2×(aA avg ) (9);

[0236] The control mechanism module performs the following operations:

[0237] Continuing filtration at a first filtration pressure value P1 for a preset time length;

[0238] The mechanical filter press pressure is regulated by the following formula until the second filter press pressure value P2 is reached:

[0239] P2=P1+r1×t (10),

[0240] r1 is the first pressure growth rate, t is the duration;

[0241] The mechanical filter press pressure is regulated by the following formula until the third filter press pressure value P3 is reached:

[0242] P3=P2+r2×t (11),

[0243] r2 is the first pressure increase rate, t is the duration, r1>r2.

[0244] Table 2

[0245] 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]]>

[0246] Example 8

[0247] This embodiment provides a dehydration method and system based on the waste agglomeration rate. Any content that overlaps with the previous embodiment is omitted. Unless otherwise specified, the following technical features apply to the previous embodiment, and vice versa.

[0248] The drying module used in the present application to provide heating or constant temperature dehydration for the waste grains is, for example, a paddle-type dehydration device or a cyclone dehydration device.

[0249] According to a preferred embodiment, Figure 3 As shown, for the waste slag that has been filtered to a first moisture content, the waste slag with the first moisture content is subjected to constant temperature dehydration at a first temperature corresponding to the relevant parameters characterizing the agglomeration rate in order to remove water and gas that affects the agglomeration rate from the waste slag until a second moisture content is reached, and then the waste slag that has been dehydrated to the second moisture content is subjected to temperature-raising dehydration.

[0250] According to a preferred embodiment, Figure 3 As shown, for the waste grains filtered to a second moisture content, the waste grains with the second moisture content are subjected to temperature-raising dehydration at a first temperature corresponding to a parameter representing the agglomeration rate. The temperature-raising dehydration process starts at the first temperature corresponding to the parameter representing the agglomeration rate and is increased to a second temperature below the critical point of combustion of the waste grains, and the second temperature is maintained until the waste grains reach a third moisture content.

[0251] Preferably, the drying module is configured to: based on the instruction indicating the first temperature transmitted by the control unit, stir the waste grains with a first moisture content while maintaining the first temperature; Figure 3 As shown, when the water content of the wasted grits 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 grits, and the second temperature lower than the critical point of combustion of the wasted grits is continuously maintained before the water content of the wasted grits 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 grits, the water content of the wasted grits is reduced to the third water content and heating is stopped.

[0252] Preferably, the drying module is configured to: based on an instruction indicating the first temperature transmitted by the control unit, for the second moisture content of the lost grits, continuously raise the temperature from the first temperature to a second temperature lower than the critical point of combustion of the lost grits, and continuously maintain the second temperature lower than the critical point of combustion of the lost grits before the moisture content of the lost grits drops to a third moisture content, or stop heating when the moisture content of the lost grits drops to the third moisture content before the first temperature rises to the second temperature lower than the critical point of combustion of the lost grits.

[0253] 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.

[0254] Preferably, the operation procedure of the waste drying system is as follows:

[0255]

[0256] Drying process:

[0257] in: is the first temperature of the waste grains with the first moisture content; is the first temperature of the second water content waste; T 表格It is a temperature calculation function based on an empirical table; and are the first and second moisture contents respectively; w3 is the third moisture content; T max is the second temperature below the critical point of combustion of the waste; T(t) is the temperature at time t.

[0258] Considering this dehydration process is the final step in the dehydration process, the maximum temperature of the second temperature range during this process cannot exceed 335°C (the critical combustion point of the dried grains). The maximum temperature of the first temperature range cannot exceed 70°C (to reduce the risk of protein denaturation in the grains). When the grains moisture content drops to the preset third moisture content, heating is stopped or the grains are dehydrated at a constant temperature.

[0259] Preferably, the third moisture content ranges from 5% to 18%. Preferably, the third moisture content is 5%, 8%, 10%, 15%, 16%, 17% or 18%.

[0260] Specifically, this embodiment provides a process for processing waste with a high agglomeration rate, and the steps are as follows:

[0261] Original waste grains detection: The initial moisture content of the original waste grains is 65%, and the agglomeration rate measured by the first detection module is 20% (the first agglomeration rate threshold is set to 15%, for example);

[0262] Mechanical filter pressing and dehydration: The first detection module sends the test results to the mechanical module. After receiving the data, the mechanical module determines that the agglomeration rate of the original waste is excessive. Therefore, it uses low-pressure slow filter pressing (for example, the parameters are set to a pressure of 0.3-0.8 MPa and a rate of 0.1 MPa / min) to process the original waste to a target moisture content (for example, set to 50%) to avoid agglomeration and hardening caused by excessive compaction. During this process, the pre-crushing blade group (the speed is set to 100 r / min, for example) cuts the initial agglomerates, and the filter plate micro-vibrates (the frequency is set to 20 Hz, for example) to loosen the particles.

[0263] Drying: The drying module first treats the 35% moisture content of the waste grains at a constant temperature of 60°C for approximately 30 minutes, reducing the moisture content to 25%. The temperature is then raised to 80°C and dehydrated to a final moisture content of 10%. After drying, a centrifugal crusher (e.g., set at 800 rpm) is used to crush any lumps formed during the drying process.

[0264] Screening and product separation: The screening module separates through a vibrating screen, and the high-fiber slag with low protein content (oversize) is preferably pneumatically transported to the pyrolysis reactor, and the organic matter-enriched slag with high protein content (undersize) is preferably packaged as feed raw materials.

[0265] This embodiment also provides a process for processing waste grains with low agglomeration rate, the steps of which are as follows:

[0266] Original waste grains detection: The initial moisture content of the original waste grains is 60%, and the agglomeration rate measured by the first detection module is 10% (the first agglomeration rate threshold is set to 15%, for example);

[0267] Mechanical filtration and dehydration: The first detection module sends the detection results to the mechanical module. After receiving the data, the mechanical module determines that the agglomeration rate of the original waste is within the standard, and thus adopts high-pressure rapid filtration (such as setting the parameters to pressure 0.5~1.2MPa, rate 0.2MPa / min) to process the original waste, with the target dehydration to the second moisture content (for example, set to 35%). The filter cloth self-cleaning device automatically cleans the pores after filtration.

[0268] Drying treatment: The drying module was started at a constant temperature of 70°C, then heated to 90°C at a rate of 10°C / min, and directly dehydrated to a final moisture content of 10%.

[0269] Screening and product separation: The screening module removes foreign matter through a photoelectric sorter, and the screened material (for example, with a protein content of 20%) is used as feed raw material.

[0270] The dehydration treatment system based on the agglomeration rate of the discarded grains provided in this embodiment realizes precise control of the agglomeration rate, optimization of dehydration energy consumption and high-value utilization of products, and provides an industrial solution for the resource utilization of distiller's grains.

[0271] Example 9

[0272] This embodiment relates to a waste grain drying system. This embodiment also relates to a waste grain processing system that uses viscosity in waste grain as a criterion for filter press grading and classification. Any overlap with the previous embodiment is omitted. Unless inconsistent, the following technical features apply to the previous embodiment, and vice versa.

[0273] Since protein and cellulose are the components with the highest organic matter content in the waste (up to 60% or more), considering the retention of protein and / or cellulose during the actual screening process (for subsequent participation in 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.

[0274] Methods for detecting organic matter content include dry burning (suitable for detecting the content of multiple organic substances), near-infrared spectroscopy (suitable for detection with relatively high precision requirements), ultraviolet spectrophotometry (suitable for detecting protein content alone), and enzymatic methods (suitable for detecting the content of cellulose, starch, or both). Based on the requirements of the organic matter detection settings, the first detection module includes relevant equipment for detecting organic matter content using the dry burning method, relevant equipment for detecting organic matter content using near-infrared spectroscopy, relevant equipment for detecting organic matter content using the ultraviolet spectrophotometer, and / or relevant equipment for detecting organic matter content using the enzymatic method.

[0275] 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, waste grains produced in different seasons, or waste grains produced by different raw materials.

[0276] 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.

[0277] 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 representing the moisture content of the original waste grains is measured by the second detection module. The first process parameter measured by the second detection module is transmitted 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 via the input terminal. More preferably, the second process parameter is a process parameter that affects the waste grains agglomeration rate. The first threshold value for each batch is input into the storage component of the control unit via the input terminal.

[0278] The control unit generates a corresponding experience table using the first process parameter, the second process parameter and the first threshold stored in the storage component. The first threshold is a dependent variable corresponding to the first process parameter and the second process parameter as independent variables.

[0279] Upon receiving the updated first process parameter and the updated second process parameter corresponding to the current batch, the control unit updates the first threshold corresponding to the current batch by accessing the experience table pre-stored in its storage module. The control unit updates the first threshold corresponding to the current batch using the first and second process parameters that are closest to the first and second process parameters of the current batch and that are present in the experience table as reference independent variables for updating the first threshold.

[0280] The empirical table for representing 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.

[0281] Table 3

[0282]

[0283] 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 based on 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 the day), the application type of Daqu, the raw materials of the wine mash, and the pH value of the original discarded grains.

[0284] The first temperature corresponding to the parameter representing the agglomeration rate can also be obtained from an empirical data table. The operator can determine the dehydration temperature based on the source of the waste and the first parameter, second parameter, or third parameter of the waste, such as Table 4.

[0285] Table 4

[0286]

[0287]

[0288] According to a preferred embodiment, the heated and dehydrated slops separated by high-fiber slops and organic-rich slops are screened in a differential separation method based on protein content to obtain the oversize material for pyrolysis and the undersize material for feed.

[0289] 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 waste grains obtained under different treatment conditions can be screened through 60 or 80 mesh screening, which does not affect the screening of crude protein.

[0290] Table 5

[0291]

[0292] In the above examples, after different filtration and heating treatments, the water content of the spent grains was significantly reduced, and the grains could ultimately be separated through 60-mesh or 80-mesh sieves. The screening process did not significantly affect the crude protein content. This demonstrates that appropriate filtration and heating treatments can not only effectively reduce the water content of the spent grains, but also achieve more efficient screening.

[0293] 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.

[0294] In addition, the undersize material used for feed is typically rich in organic matter and crude protein. After screening, the crude protein content of the slag can be maintained at a high level, such as 17.6% in Example 3. This makes the undersize material more suitable as feed or feed additive, thereby improving the nutritional value of the feed. By implementing the above-described 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, ultimately achieving efficient utilization of the slag in pyrolysis and feed. This method combines well-known technologies such as filter pressing, heating, and screening, and has significant technical effects and practical application value.

[0295] 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 on 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 having to be set, so 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 raw waste grains provided in batches by solid-liquid separation, wherein waste grains having a first moisture content and a second moisture content having different moisture contents are provided in a manner related to relevant parameters used to characterize agglomeration rate, wherein the first moisture content is greater than the second moisture content; S2 dehydrates the spent grains by removing moisture and gases that affect the agglomeration rate, wherein: S2.1: for the waste grains filtered to a first moisture content, dehydrating the waste grains at a first temperature corresponding to a parameter representing the agglomeration rate until the first moisture content reaches a second moisture content, and then increasing the temperature to dehydrate the waste grains dehydrated to the second moisture content, or S2.2: For the waste grains filtered to the second moisture content, the waste grains with the second moisture content are heated and dehydrated. The heating and dehydration process starts from the first temperature corresponding to the parameter characterizing the agglomeration rate and continues to heat up to a second temperature lower than the critical point of combustion of the waste slag, and maintains the second temperature until the waste slag reaches a third moisture content. S3 screens the heated and dehydrated slops separated from the high-fiber slops and the organic-rich slops by differential separation based on protein content, obtaining the oversize material for pyrolysis and the undersize material for feed.

2. The method for drying the waste grains according to claim 1, wherein: In the S1 step, the mechanical module for mechanically pressing and dehydrating the original waste dregs produces an extrusion effect on the original waste dregs 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 intercepts the solid matter in the original waste dregs and transfers the solid matter 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, wherein: In the step S1, the mechanical module mechanically filters the original waste grains in a manner of a preset first threshold value of a parameter related to 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, wherein: In the S2 step, the drying module provides heat to the waste dregs which are transferred 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 dregs with the first moisture content by removing the capillary water and bound water distributed in the solid matter in the waste dregs in a manner that reduces the agglomeration rate of the waste dregs.

5. The method for drying the waste grains according to claim 1, wherein: In step S1, the second detection module for detecting the moisture content of the original waste grains collects the moisture content of the original waste grains and transmits it to the control unit, wherein, according to formula (1), the control unit for generating the corresponding waste grains drying treatment method calculates the first moisture content M1 of the original waste 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 moisture content of the original waste; k1 represents a constant; a represents a first threshold; and 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 step S1, the second detection module for detecting the moisture content of the original waste grains collects the moisture content of the original waste grains and transmits it to the control unit, wherein, according to formula (2), the control unit for generating the corresponding waste grains drying treatment method calculates the second moisture content M2 of the original waste grains for which the relevant parameter characterizing the agglomeration rate is lower than the preset first threshold value based on the moisture content transmitted by the second detection module: M2=b-k2×(a-A2) (2), b represents the moisture 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 among the relevant parameters for characterizing the agglomeration rate is set to be 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 slag presses the original waste slag whose first parameter exceeds or is equal to the preset first threshold to the 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: At least one of the parameters used to characterize 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 used to characterize 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 using formula (3):

10. The method for drying the waste grains according to claim 1, characterized in that: In the processing step S2, the dehydration treatment includes the following steps: using the reduction of the moisture content of the slag to a third moisture content that can be used as dry feed as a judgment basis for stopping the dehydration treatment, and performing a dehydration treatment on the slag that has been filtered to the first moisture content and whose moisture content has been reduced to the second moisture content, or the slag that has been filtered to the second moisture content, by raising the temperature from the first temperature to a preset maximum temperature value.

11. The method for drying the waste grains according to claim 1, characterized in that: When the provided waste grains have a first moisture content, they are dehydrated at a first constant temperature until they reach a second moisture content, and then the temperature is increased from the first temperature until the waste grains reach a third moisture content; if the third moisture content has not been reached by the critical point of combustion, they are dehydrated at a constant temperature before the critical point of combustion until the third moisture content is reached.

12. The method for drying the waste grains according to claim 3, characterized in that: In the processing step S1 , the relevant parameter characterizing the agglomeration rate may also be a third parameter represented by a pressure value, and the first threshold value may be set as the pressure parameter.

13. A waste grain drying treatment system, characterized in that: The system comprises a mechanical module for mechanically filtering and dehydrating the original waste, a first detection module for detecting at least one parameter of the parameters representing the agglomeration rate in the original waste, a drying module for heating the waste at a constant temperature or at an elevated temperature, and a screening module for screening the dried waste, 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 used to characterize the agglomeration rate of the original waste grains detected by the first detection module exceeds or is equal to 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 exceeds or is equal to the preset first threshold value to a first moisture content, When at least one parameter characterizing 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 characterizing the agglomeration rate, the mechanical module presses the original waste grains having the relevant parameter 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 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 representing 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 representing agglomeration rate; The screening module screens the heated and dehydrated slop separated from the high-fiber slop and the organic-rich slop in a differential separation method based on protein content to obtain an oversize material for pyrolysis and an undersize material for feed.

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