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    • 专利摘要:
    In order to achieve a better fermentation in the comminution of lignocellulosic feedstocks, the systems used have a high own energy consumption, in particular power consumption for the mechanical drive. Consequently, the achievable increase in efficiency is low or often even questionable. In addition, it does not sufficiently succeed in unlocking the lignin content. To solve this problem, a device for generating a biomass propagation is provided which has a device for introducing a difficult-to-open biological starting material (50), wherein the difficult-to-open biological starting material contains lignin, an activator (42, 70) for digesting the educt, which is activatable when a temperature TA is exceeded, with TA> 55 ° C, wherein the activator thermophilic microbes in a concentration of more than 1 million per milliliter, which are activated from the temperature TA, and a means (21) for thermal activation comprising a combination of starting material and activator.
    公开号:AT14738U1
    申请号:TGM351/2014U
    申请日:2014-10-08
    公开日:2016-05-15
    发明作者:Matthias Wackerbauer
    申请人:MWK Bionik GmbH；
    IPC主号:
    专利说明:

    description
    The invention relates
    DEVICE FOR PRODUCING A BIOMASS PREPARATION, ESPECIALLY OF HIGH-LIGNIN INGREDIENTS
    [0001] The present invention relates to a device for producing a biomass composition (biomass composition), in particular a fermentable biomass addition, by a combination of biological, mechanical and / or thermal activation of microbiological activators capable of difficult-to-open biological products, in particular the lignin content of biomass, digest and fermentable.
    Conventional biogas plants work with hydrolyzing and methanizing bacteria that can metabolize sugars and other easily fermented carbon compounds to methane. However, such biogas systems have the disadvantage that they in particular ligninhaltige feedstocks such. For example, straw does not ferment or hardly or only very slowly ferment. In view of the finite residence time of the biomasses in the fermenter, which is finite for economic reasons, up to more than 50% of the biomasses thus remain unfermented in conventional biogas plants. This means a considerable inefficiency and leads to high feed consumption. In times of high feedstock prices, this is economically very disadvantageous and jeopardizes the profitability of conventional biogas plants.
    Thermophilic biogas reactors have also been developed which ferment at higher temperatures. As a result, the digestion and methanation of the poorer fermentable constituents of matter become somewhat better. However, substantial proportions of biomass remain fermented. In particular, strawy biomasses lead to the formation of floating layers in the repository, even if the total yield already accounts for more than 50% of the carbon input. Vegetable biomass consists in particular of cellulose, hemicellulose and lignin. Lignocellulose is protected by a lignin layer and therefore can not or only very slowly be fermented without further pre-treatment.
    In recent years, numerous systems have been developed to achieve a better fermentation by Zer¬kleinerung of the starting materials. However, these systems each have a high inherent energy consumption, in particular power consumption for the mechanical drive. Consequently, the thus achievable increase in efficiency is low or often even questionable. In addition, it also succeeds not sufficiently to unlock the lignin.
    Also, biological and biochemical substances and methods for optimizing the fermentation metabolism in the biogas plants have been developed. These methods help to remedy deficiencies in the metabolism of microbes and can increase the yield. However, this does not change much in the generally poor fermentability of the woody and / or lignin-containing feedstocks. This problem of scarcely possible straw fermentation is all the more serious since up to 50% and more of the feedstocks such as maize silage consist of straw-like biomass. With conventional technology so typicalca remains. 50% of valuable biomass used without fermentation. When using high straw biomass such as horse manure, fermentation is often very difficult and inefficient.
    Therefore, activation methods have been developed in recent years, with the steam works. The problem here is that steam must be generated directly at the biogas plant, which means a lot of effort. It has been found that even after steam digestion the overall efficiency of methanation can not be increased sufficiently.
    So far unsatisfactory solved the most complete digestion of ligninhaltigerBiomassen such. B. Strohanteilen, in order to achieve a much more complete fermentation of the biomass used in this way. The process should also be efficient, safe and cost effective.
    Lignin consists of solid biopolymers which are incorporated into the plant cell wall and thereby cause the lignification of the plant cell. Lignin is responsible in particular for the compressive strength of plant constituents, so it is found in the stem or stalk and / or in the skins.
    The natural biodegradation of lignin is very slow and is biologically complex. The lignin degradation always takes place under aerobic conditions and is very energy intensive. Accordingly, it can not serve as the sole source of carbon and energy. The natural degradation of lignin can therefore not be used for biomass energy plants.
    The technical Ligninabbau plays an important role, especially in pulp production. To produce pulp, the lignin from the lignocellulose must be dissolved and removed from the process. There are different methods for the Celluloseauf¬schluss and for subsequent pulp bleaching. In about 80% of all pulp plants, the digestion takes place via the so-called sulphate process, also known as the kraft process. An alternative is cellulose digestion in the sulfite process, where lignin degradation is by sulfination.
    DE 10 2005 030 895 A1 describes a device for disrupting biological material held in dispersion with a vessel for passage of the material in which a group of discrete sound generators is introduced. In particular with ultrasound. The device should serve to shred the pieces. The thermal energy input by the ultrasonic generators is sufficient to allow the downstream fermentation to occur at the appropriate temperature. The device is described in connection with a fermenter and biogas utilization in a combined heat and power plant (CHP). The description mentions an introduction of the prepared mass from below injected under high pressure, because of intentional intensive mixing in the fermenter.
    DE 10 2011 113 646 B3 describes a digestion container for bale intake and supply of a preheated acid / water mixture via injection devices and sieve elements in the bottom region for separating the liquid hydrolyzate from the solid biomass. The activation preferably takes place at 140-160 ° C. Mineral or organic acids are used. Dissolve 50% of lignin. Hemicellulose is converted to more than 75 monosaccharides.
    DE 31 38 309 A1 describes a process for the digestion of wood and other lignin-containing substances, wherein the animals living in the intestinal tract are used, as they are found especially in termites in symbiosis. It is also mentioned that the primordial animals and bacteria are deep-frozen or freeze-dried after their separation and multiplication.
    DE 10 2011 118 067 A1 describes an activation process wherein acetic acid formers are added. The activator initiates formation of acetic acid, promotes it and maintains acetic acid formation. The term acetic acid is also to be understood as meaning acetates, the salts of acetic acid. Because in biochemical processes mostly the anion CH3COO " in front. It forms the so-called acetic acid acetate buffer. Living acetic acid bacteria are used and a suspension is prepared from sugar, alcohol and water, which is typically added at 1 liter per cubic meter of biomass. Alternatively, live yeast is added. The reaction takes place at a pH of less than 4. The device uses spiral-shaped agitators.
    DE 198 58 187 C2 describes a method and a device for reducing the organic content of an expandable substrate. In this case, a first anaerobic digestion is combined with a thermal disintegration and with a subsequent second anaerobic digestion step. Despite the expense of thermal disintegration, however, only the hemicellulosic digestion succeeds, but the lignin portions remain unresolved. The yield of energy only increases by about 10%.
    Although all these known methods indicate that they can also digest lignin, they only manage this in a very small and economically unprofitable manner. This makes lignin degradation in fermentation plants so far technically and economically inefficient. Consequently, the lignin-containing parts of plants remain unused and so far land in the digestate (in biogas plants up to 50% of the biomass).
    The object of the present invention is therefore to provide a device for producing a biomass preparation, wherein also biomasses with a very high lignin content wiez. As cereal straw, horse manure, green cuttings of woody plants, digestate and or miscanthus or C4 grasses as starting materials (starting materials) can be used while the enthalte in the starting material organic carbon as completely as possible in high-energy hydrocarbons (eg., Methane) converts becomes.
    This object is achieved by a device for generating a Biomassezube¬reitung, comprising: - A device for introducing a hard aufschließbaren biological starting material (starting material), - an activator for digesting the starting material, when exceeded a temperature TA is activated, with TA > 55 ° C., and [0021] a device for thermal activation of a combination of starting material and activator.
    The device for introducing can bring in the difficult-to-open biological starting material, for example, in liquid, pasty and / or solid form.
    The apparatus may further comprise: means for increasing or increasing the volume.
    The means for increasing the pressure and / or volume delivery may comprise, for example, a pump and / or a compressor.
    In a further embodiment, the device according to the invention for generating a biomass preparation comprises: a) a device for introducing difficult-to-open biological educts, in particular with a high lignin content, b) a device for adding and mixing an activator / activator for breaking up the starting material (s), the activating agent being activatable at excess temperatures of TA, with TA > 55 ° C, optionally with the additional condition pressure P> PA with PA > 1.3 bar, c) a device for activating a combination / mixture of starting material (s) and
    Activator by increasing the temperature to T> TA at pressure P> PA, d) a device for increasing the pressure and volume, in particular a
    Pump or a compressor, preferably arranged in the flow direction in front of the device for Akti¬vierung.
    The device according to the invention processes hard-to-disintegrate, especially lignin-containing, starting materials and makes it possible to produce a high-quality biomass preparation in which the lignin is also digested to a large extent. It is ideally suited for use in bio-refineries or biogas plants.
    The activator comprises a mixture of microbiological components, preferably incorporated in a liquid and optionally supplemented by nutrients and nutrients.
    The microbiological activator / activator according to the invention contains large amounts (more than 108 particles / microbe per milliliter, preferably 101 ° to 1012 per milliliter) of thermophilic pressure-loving microorganisms. Particularly preferred activation conditions are temperatures between 65 and 85 ° C and pressures between 2 bar and 6 bar. The activator consists of a mixture of microbiological components, preferably incorporated in a liquid.
    The activator is, for example, a suspension containing more than 1 million particles per milliliter, preferably more than 1 billion particles per milliliter. It preferably contains both aerobic, as well as anaerobic and thermophilic microorganisms. A proportion of these microorganisms is solvent-forming agent, i. H. The organisms produce locally on the surface of the Einsatzstoffpartiεkel solvents that attack the previously difficult aufschließbaren layers and detach the lignin. The presence of the solvent-forming agent is mandatory.
    Preferably, the solvent-forming agent is the thermally activated microbiological component. A distinction should be made between activatable solvent formation and the absence of solvent addition. The activatable formation of the solvents takes place according to the invention microbiologically, ie by primordial animals (archaea), bacteria and / or fungi. It is also necessary to distinguish between the solvent formed after activation at the biomass interfaces and the solvents used in other technologies. The microbiologically produced after Akti¬vation solvents lead z. B. initially only for detachment of the lignin layer, but not yet for the dissolution of the lignin. Only after detachment are the lignin fragments broken down by microbes into short chain carbon compounds.
    The educt can be used in solid, slurry or liquid form, so that almost all possible biomasses, such. As straw, plant stems, wood chips, animal Ex¬kremente, slaughterhouse waste etc. can be digested.
    The device according to the invention may comprise a device for bringing the educt (s) into contact with the activator, for example a mixing chamber, but in a further embodiment it is provided that the educt is already in accordance with the invention before it is introduced into the egg Device is brought into contact with the activator, z. B. mit¬tels spraying the starting material with a liquid activator.
    The device according to the invention for thermal activation comprises a device for controlling the temperature of the educts or the biomass preparation to a temperature above the activation temperature T> TA. Preference is given to heat exchangers are used, thez. B. be heated by engine waste heat of a nearby cogeneration plant. Heating of the reactants mixed reactants initiates activation. Preferably, the activation is assisted by the application of an increased pressure level, the pressure being higher than the activation pressure P> PA. The temperature increase may in particular embodiments also be caused by internal chemical heat sources, e.g. As by-passing exothermic reactions or by electrical heating or by irradiation of electromagnetic waves or sound. Further alternatives are explained in more detail below with reference to the figures.
    Further embodiments of the device according to the invention further comprise a mixing device for educts, which is designed so that different feedstocks with different physical states, solid, papery or liquid, can be premixed, such. B. a pure solid premixer or a solid-liquid feed mixer.
    In some embodiments, the device according to the invention has a device for heat recovery, so that the device according to the invention can be operated particularly energy-efficiently. In this case, thermal energy is preferably transferred from the product auflos¬senen on at least one of the starting materials in order to increase its temperature.
    The various embodiments of the device according to the invention can be described as a combination of a biological, mechanical and / or thermal-acting device: A biological device for metering in microbiological
    Activation substances (of the activator), which can attack lignin-containing layers above a certain minimum temperature, - a mechanically acting device for the supply of hard aufschließba¬ ren starting materials (educts) and mixing with the activator, wherein a be¬stimmtes pressure level [0044] - as well as a thermally acting device for setting a temperature above the activation temperature, whereby the activation of the activator is achieved and the microbiological digestion of the lignin is started.
    In a further embodiment, the device according to the invention may comprise the following components: - a device for preparing a biomass mixture, e.g. Solid-liquid feed system, pre-fermenter, hydrolysis step or disintegration step, wherein at the exit a mass flow of lignocellulosic biomass is made available, - a device for the metered supply of an activating agent which is first activated by
    Achieve or present an activating range in pressure, temperature and nutrient concentration and time is activated.
    [0048] a device for adjusting a pressure z. B. 4 bar and for promotion, z. B.
    Pump or compressor, a device for adjusting a medium temperature, for. B. heat exchangers or
    Heating or internal biochemical heat release.
    The device according to the invention can comprise in a further development two heater systems, namely a preheater and a reheater. The pre-heater liquid feedstock heats up to a premix temperature Tv. The preheated liquid feed is admixed with a solid feed formulation which is preferably particulate, e.g. B. chopped or ground straw. The resulting mixing temperature is TM. The mixed feedstock is treated with activating agent before or after mixing and then heated to T> TA through a reheater. This leads to the activation of the activator and consequently to the microbiological detachment of the lignin and further to the microbiological decomposition of the lignin.
    The device according to the invention can in a development two pump systems, which serve the pressure increase and volume promotion, comprise, namely a first system zumaufbau a working pressure and a second pump system for generating a Zirkula¬tionsströmung. The circulation flow is preferably used to flow through the preheater with flüssi¬gem feedstock.
    The device according to the invention may comprise, in a further development, three heat exchanger systems, at least two pumps, a separator for the provision of separator fluid and a solid biomass feed system with the admixture of fluid or liquid biomass.
    The three heat exchanger systems are preferably designed so that they each can transmit up to 50 kilowatts of heat output, based on a firing heat output of 500 kilowatts. The first heat exchanger acts as a preheater, the aufca from the recuperator aufca. 50 ° C preheated separator fluid heated up to 80 ° C in circulation mode. The fluid flows through a circulation pump at a high pressure level of about 4 to 10 bar. The second heat exchanger functions as a reheater, the mixture of biomass / activator again heated to temperatures of more than 75 ° C, preferably 80 ° C to start the lignin digestion. The third heat exchanger acts as a recuperator for the recovery of heat and transmits z. B. in countercurrent, the heat of the present invention digested Biomasse¬ preparation on the provided separator fluid, the liquid feed fraction. This is important to limit the heat input into the fermenter. The heat exchangers are preferably configured as tube jacket heat exchangers. In the continuous inner tube each of the higher viscous fluid flows. The outer tube is preferably coiled and has two flanges for inlet and outlet. The total heat input is about 6% to 20% of the Feuerungswärmeleistung.Die heat can z. B. be made available regeneratively over the engine cooling water of a CHP.
    The pressure generation and promotion of feedstocks with high dry matter content is technologically difficult, especially at high temperature above 60 ° C. Thus, a particularly preferred embodiment of the apparatus of the present invention employs a pressure generating pump which compresses cool fluid feed at T <50 ° C to a pre-pressure Pv of e.g. B. 4 bar to 6 bar. Only then does the heating of the fluid feedstock take place. Due to the increased working pressure, the gas release is prevented. The working pressure is further used as the predominant driving force to move the mass through pipes, mixers, valves and heat exchangers, etc.
    The preheating of the feedstock fluid is supplemented by a further Wärmetau¬scher, which has the ability to bring the fluid for heat absorption even without interference promotion of fluid in the Einsatzstoff mixer. Particularly preferred is a circulation heating circuit driven by an additional circulation pump which is at circuit pressure Pk. The pump delivers pressure from Pkr to Pkv. The pressure drop in the heating circuit takes place via pipes, distributors, heat exchanger valves, etc.
    The access to the fluid entry into the feed mixer is completed by at least one valve V which can be varied in its opening. The circulation circuit also has a valve Vk which releases or shuts off the circuit. The first position is the filling of the circuit with closed circuit valve Vk and open entry valve Ve. The second position is the recirculation position with open circuit valve Vk and closed entry valve Ve. Mixed positions in between are possible and sometimes beneficial.
    A development of the invention further comprises a feedstock mixer for solid Ein¬tragsstoffe, optionally provided with activator, and fluid feedstocks, preferably preheated. The feed mixer comprises a compression section with motor drive, which forms a liquid-tight plug of feedstock and imitates continuously, to the extent solid feed is mixed in the feed mixer. The continuously formed and spent plug causes a pressure-tight seal against the liquid feedstock supplied under pressure and against the activation regions in which the mixed feedstock is thermally activated.
    In a special development, the tightness of the plug is ensured by a novel control technology. The hitherto customary control technology regulates the speed of the pressure generating pump. Surprisingly, however, we found that this does not provide the desired security against breakdown of the liquid against the conveying direction. According to the invention a control valve is now regulated in the feed fluid inlet and, optionally, a shut-off slide is connected in series for safety, whereby the flow is rapidly reduced if the tightness of the feed mixer is no longer present. The feed mixer automatically generates by its action a continuously consumed feed plug which has sealing properties. These sealing properties are the better the better the mass can be compacted, so that no fluid channels remain.
    In a further development, the device according to the invention comprises a supply of gel-forming agents to the dry feedstock. For in a test situation with poorly sealing starting materials, we surprisingly found that the addition of gel-forming agents into the premixer in the mixture of the solid feedstocks or else in the feedstock mixer itself has the effect of forming particularly pressure-tight stoppers. This embodiment thus comprises a feed mixer with gelling agent delivery device. Suitable gelling agents are e.g. Chitin or chitosan preparations or oils or jelly-like preparations, especially those which become liquid at elevated temperatures and jelly-like at temperatures below 60 ° C. The quantities added cause the
    Fluid channels are sealed in the stopper. However, the plug is always consumed during operation and the material is mixed in. So you have to constantly mix new gel formers.
    In the device according to the invention, a process for producing a biomass preparation preferably takes place, comprising the steps: a) providing a poorly digestible biological starting material, b) providing an activator for breaking up the educt which, when a temperature is exceeded TA is activatable with TA &gt; 55 ° C, and c) activating a combination of reactant and activator by means of a device for thermal activation.
    The method may further comprise: d) providing a means for increasing or increasing the volume.
    The object of the present invention is further achieved by a method for producing a biomass composition comprising: a) providing sparingly digestible biological starting materials in liquid and / or solid form, [0068] b) contacting Bringing the reactants / the starting material with an activator / Aktivie¬ means, c) activating the activator by heating the combination activator &amp; Educt on one
    Temperature TA by means of a device for thermally activating the activator, d) optionally supplemented by pressure generation to a pressure P &gt; PA means of Druckhö¬ hungsvorrichtung, z. B. pump or compressor, z. The method advantageously allows, but is not limited to, the particularly efficient production of fermentable biomass compositions, particularly, but not limited to, the digestion of lignin-containing products.
    The method is based on the predominantly thermally activatable effect of a microbiological activator, which can be further enhanced by the application of elevated pressures. This activator differs quite significantly from all previously used agents.
    The microbiological activator used in the invention contains large amounts of approx. 100 billion particles per milliliter of thermophilic pressure-loving microorganisms. Particularly preferred activation conditions are temperatures between 65 ° C and 85 ° C and pressures between 2 bar and 6 bar.
    The activator is optionally already added to the solid feedstocks in the premixer. Alternatively, the activator is already part of one of the feedstocks which are mixed in the feedstock mixer. The activator is z. B. the solid feed such. B. straw, z. B. by spraying from a nozzle device. In this case, the activator comes into contact with the surface of the feedstock particles.
    Another alternative is to feed the activator directly into the pipeline into the mixed feed.
    Two different microorganisms are preferably used: Anaerobic or aerobic microbes which break up and degrade biomolecules (for example proteins, sugars, fats, celluloses, nucleic acids), which are therefore z. B. can digest the long-chain Zellulo¬sen and convert into shorter-chain molecules.
    Thermophilic microbes which produce release agents above an activation temperature, e.g. B. detach the lignin layers of the biomass particles.
    In particularly preferred activating agents, more than three different types of microorganisms are used.
    - Anaerobic microbes that break up and break down biomolecules, so z. For example, they can digest the long-chain celluloses and convert them into shorter-chain molecules.
    - Aerobic microbes that drive metabolism with the help of oxygen and or oxidizing agents.
    Thermophilic microbes which generate release agents above an activation temperature, which z. B. detach the lignin layers of the biomass particles.
    An embodiment of the activating agent combines the above-mentioned mixtures of microbes with trace elements.
    A particular embodiment of the activating agent combines the above-mentioned mixtures of microbes with gelling agents.
    A further particular embodiment of the activating agent combines the above-mentioned mixtures of microbes with auxiliaries for enhanced exothermic reactions, which subsequently contribute to the heating of the starting material mixture.
    The thermal activation takes place by exceeding an activation temperature T at least the activation period Za. In this case, the actually achieved temperature is the decisive factor for how long the activation time Za must be at least in order to unlock the hard-to-digest fractions. At the present time the lowest temperature is Ta = 63 ° C, but then it takes hours of activation time. Technically, actual temperatures of Tt = 70 ° C to 75 ° C are necessary to achieve activation within a short time. Contrary to first assumptions, the activation temperature is not sharply limited, but sliding. There is a relationship whereby twice the excess temperature Tt-Ta results in at least halving the activation time Za. Technically, the actual time Zt of exceeding Ta will be longer than Za. Side effect of the thermal activation is usually also a sanitation of the feed.
    The solid starting material, for. B. straw, is advantageously mechanically crushed before the solid-liquid mixture. The mechanical comminution of the starting material and the subsequent mixture with the added activating agent is carried out according to the invention. Optio¬ nal a working pressure of more than 1 bar is generated, preferably more than 2 bar or more than 3bar to suppress the formation of gas and to increase the gas solubility.
    The pressure increase is not absolutely necessary, arise at atmospheric pressure and often escape C02 and NH3. Characteristic of the invention is therefore in particular the pressure-resistant closed system in the area of heating. The solids entry is of course open. Here is how technically usual z. B. poured straw through a funnel in a Feststoffstoffeinbütschapparat. However, the solid feed is liquid-tight and pressure-sealed against the heating area or areas. The pressure release takes place only after the thermal activation, in particular after pressure reduction by friction losses in the pipe when leaving the pipe end in the fermenter.
    The method is carried out in a further embodiment as follows: The preparation begins with the provision of a mixture of lignin-containing predominantly organic dry substance biomass. This is preferably tempered to about 20 ° C to 30 ° C and optionally previously brought into contact with the activating substance, for. B. by sprinkling etc.
    The mixed dry substance is compressed in a solids feed and mixed with a supplied fluid stream. This succeeds z. B. with the EnergyJet the Fa. Vogel¬sang or with other, the skilled person known mixers.
    The supplied fluid stream is preheated to about 80 ° C. This is done by stepwise heating, preferably with heat recovery and in circulation systems.
    In further embodiments of the method in the device with circulation, the method can be carried out in a clocked manner (see FIG. 5).
    In cycle A liquid feedstock is conveyed into the circulation, wherein the circulation valve is closed and the inlet valve (43) and the metering valve (42) are open. At the same time, the booster pump and the circulation pump are active at the same time. The preheated feed flows to the feed mixer (9) for mixing with the solid feed. The same hydrostatic thrust promotes, step by step, the mixed feedstock through the thermally activating heat exchanger (23) and further through the recuperator (21) to the fermenter. In this case, optionally further conveyor systems can be installed if the pressure drop requires it.
    In cycle B, the inlet valve (43) is closed, the circulation valve (41) is opened and the metering valve (42) is closed. Consequently, the entire circulation line is under a working pressure and the liquid feed is circulating through the circulation pump until a desired preheat temperature is reached. Then again clock A.
    The mixture produced in the feed mixer has already partially reached the mixing temperature above 70 ° C. It is further heated to temperatures up to 80 ° C in order to exceed the activation temperature as long as possible in all volume elements of the biomass preparation. This can be z. B. by means of heated by engine cooling water Nacherhitzerwärme¬ exchanger, as described above.
    Optionally, then a cooling of the biomass preparation take place. In order to avoid overheating of the fermenter, usually a cooling, z. In a recuperator.
    The biomass composition thus produced from lignin-containing biomass can subsequently be used in biorefineries and biogas plants as a very high-quality feedstock.
    The microbiological activation takes place in the reheater and after. The activation according to the invention first leads to the microbiological detachment of lignin and subsequently to the microbiological digestion of lignin. The digestion reaction continues to run even when the temperature drops again and also when the pressure drops again, to the residence time in the subsequent fermenter. The activation must therefore have taken place only over a minimum duration of preferably a few seconds, so that the microbiological digestion of the lignin can proceed subsequently. As a result of the digestion of lignin, a corresponding excess amount of bioenergy energetics, e.g. B. generates biomethane.
    Furthermore, the inventive reduction and activation of Einsatz¬stoffe the electrical energy consumption for agitators, separators and other auxiliary equipment is significantly reduced. Overall, therefore, under favorable conditions, the digestion of the lignin can be done with very little additional electrical energy. This is economically and ecologically of great advantage.
    Figures and embodiments The invention is explained in more detail below with reference to exemplary embodiments and figures, without this being to be understood as limiting to a specific embodiment.
    [00103] FIG. 1 shows a diagram of the apparatus according to the invention, [00105] FIG. 2 shows an embodiment of the apparatus according to the invention with a filler mixer for solid feedstocks, [00106] FIG. 3 shows an embodiment of the apparatus according to the invention 4 shows an embodiment of the device according to the invention with a device for heat recovery, and [00108] FIG. 5 shows a further embodiment of the device according to the invention in a schematic view.
    FIG. 1 shows various starting materials (50, 51... 55) which are made operational in a preparation device 61-62. These preparation devices 61-62 can be, for example, solid-liquid feed mixers such as EnergyJet, liquid-liquid feed mixers, pre-fermenters, hydrolysis stages or thermal disintegrators or separation devices. In general, a pumpable flowable and heat-conducting biomass material (1) is thus made available which has an economically interesting content of lignin-containing biomass which is difficult to digest (in the case of conventional systems, up to 60% or more of the feedstock content of Strohal's feedstock) not unlockable in the residence times relevant for economic installations). Typical of the biomass material (1) are 30% to 80% of the organic substance as lignocellulosic biomass. In order to facilitate the possible decomposition of lignin and thus the further release of energy sources such as CH4 (methane), an activator is added and then activated. Basically, the addition can already take place in the preparation stage (61-62); it has to take place at the latest before the activation stage (21). The entire activation device consists of several elements (41, 31, 21, etc.) and produces the appropriate activation conditions. The addition of activator thereby creates the biological preconditions (by the addition of thermophilic activating microorganisms which produce locally on the lignin biomass releasing biochemicals can be supplemented as needed with excipients such as trace elements). The addition of the activator takes place by means of metering system in quantities of typically 0.1 to 10 liters per tonne of total biomass. The dosing system (41) is optionally configured to also dose to the elevated activation pressure level (eg, 4 bar). After dosing biomass and activator is mixed and contacted, z. By the mixing action of a solid-liquid feed system (e.g., EnergyJet) or the mixing action of a fluid pump (e.g., centrifugal pump). In addition to the mixture, an increase in pressure to activation pressure greater Pa is also carried out in this conveying element (31). In addition, a temperature increase to activation temperature greater Ta is made. For the temperature increase, a heating element (21) is used selected from (heat exchanger, heating cartridge, internal reactive heat source, eg, exothermically reacting additives). After activation (at the latest beginning in activation device 21), the lignin-containing biomass is first detached and then the lignin-containing biomass is dissolved step by step, with the otherwise difficult-to-open biomass being converted into a fermentable mixture of substances, which in particular contains short-chain carbon compounds.
    FIG. 2 shows a device according to the invention with feed mixer, here designated as (9). The mixer (9) generates the feedstock (1) for the actual activation system. It can also be seen that the position of the pump (31) is set in the fluid circuit. The decisive factor is the pressure downstream of the mixer (9) and in the thermal activation device (21) P &Gt; Pa and T &gt; Ta must apply. The then activated starting material is hereby marked (58).
    The activator stream (42) is added to the feedstock stream, optionally in the feedstock mixture (50, ..., 55) or in the feed mixture (1) produced therefrom. In addition, the feedstock (1) is pressurized to P &peseta; Pa and brought to temperature T &gt; Ta. As a result, the activation is achieved and the microbiological components of the activator (42) begin to become active. After activation, a reaction path takes place, in which case the temperature can already be lowered again, but not necessarily. Temperature reduction by e.g. Rekupera¬tor is optionally used in mesophilic fermenters to limit a temperature increase in the subsequent fermenter. For thermophilic fermenters can be z. For example, do not cool down after activation. A particularly preferred embodiment uses to produce the feed mixture (1) a proportion of solid digestate, preferably from the repository. These are z. B. separated by a separation device (filter, separator, etc.) and brought to the feed mixer and mixed there with straw. Another particularly preferred embodiment makes use of a proportion of liquid fermentation residues or fermenter contents having an org.drying substance content typically below 10%, preferably below 6%, especially below 4%, in order to separately heat up, compress and provide the activator with this fluid fraction Mixing with the dry-solid feeds in a suitable mixing device such. B. EnergyJet from Vogelsang. The resulting feed mixture is already activatable by the addition of the activator and by the mixture. The form can also be used to at least partially build up the activation pressure. The flow temperature Tv obtained after mixing is also a good starting point for the further heating above the activation temperature Ta. In the special case, the mixer flow temperature Tv even reaches to reach the activation temperature Ta. As a rule, however, a further heating section is connected downstream in order to exceed Ta.
    Heating either by heat exchange z. B. with engine cooling water or by Elekt-roheizer with excess flow or by contained exothermic reagents.
    It is also particularly preferred to guide the low organic content fluid (OTS) in a preheating device, e.g. B. Wärmetauscher¬ circuit, at an elevated pressure level Pv, which is above the activation pressure Pa.Dazu a pressure booster stage (31) is used and optionally another Umwälzvorrich¬ tung (32). The addition of the activator (42) is optionally carried out before the feed mixer (fluid side or solids side uses the mixing effect) or after the feed mixer (but then combined with subsequent activator mixer as part of (41)), but in any case before thermal acting activation device (21). The activator (42 or 70) may also be added after the mixer (9), but this is not advantageous, because then an additional activator-mixer (41) would be necessary. Preferably, the addition of the activator (42) is before the feed mixer (9) and into the system (61-62) in Fig. 2, respectively, because then the mixing action of the feed mixer is used for intimate admixture with the activator (42 or 70) ,
    FIG. 3 shows a further embodiment of the device according to the invention with a device for mixing solid and liquid starting materials. After the mixer 9) the feed (1) is available for activation. The preheating of the fluid feedstock (53) over a thermal distance (22), z. Example, a heat exchanger or a Heizele¬ment, optionally extended by circulating circuit with conveyor 32. The activation pressure is preferably constructed by a pressure booster stage or conveyor (31). The heating path (21) ensures that at least T> Ta is reached everywhere in the feedstock. The activated feedstock (58 or 2, respectively) enters the reaction zone where the detached lignin microbiological is dissolved. Optionally, the temperature of the activated starting material is reduced or reduced thereafter. FIG. 3 shows further special pump arrangements. The conveyor (31) already generates the high working pressure. Conveying device 32 serves to circulate the fluid feedstock (53) in the preheating circuit including the thermal line (22), which can be designed, in particular, as a heat exchanger, heated, for example. By engine waste heat.
    Instead of a heat exchanger as an embodiment for the heating section (21 and or 22), electrical heaters or biochemical reaction components which lead to heating can also be used. All that is essential is that in these heating sections a thermal state T> Ta is reached and maintained over time Z> Za.
    The use of a heat exchanger can be dispensed with if, after the admixture of the activator, the feed mixture is brought to an eligible consistency, e.g. B. by mixing with fluids, and before and / or thereafter due to special Wär¬mefreisetzung to an actual temperature Tt above the activation temperature Ta brought and at least the time Za is maintained at least this temperature. The particular heat release can z. B. by exothermic reactions, as z. B.unter¬ use of introduced oxidizing agents and or other reagents can suc. The introduction of oxygen z. B. happens in the solids supply from the atmosphere and it can be added additional reactive agent.
    FIG. 4 shows a further variant of the device described in more detail in FIG. This now also has a device for heat recovery (Rekupera¬tor). The feed mixture initially has a high temperature greater than Ta after activation and thus carries much specific heat. This heat can z. B. are discharged to preheat the feedstock fluid. It is therefore a heat recovery that reduces the heat consumption of the system. In addition, the heat input into the fermenter is reduced. Preferred temperatures after the recuperator are z. B. 55 ° C. Compared with the embodiment shown in FIG. 3, the device according to FIG. 4 thus has a recuperator (23) for recovering the heat from the activated starting material (58). The recovered heat can be z. B. for preheating the fluid feedstock (53) verwen¬det. In a further embodiment, the recuperator (53) can also heat a simple cooler.
    Figure 5 shows a schematic structure of a device according to the invention. In this particular embodiment, in particular the floating of chopped straw by activation and mixing of lignocellulosic biomass with activating fluid and recycled material in the device for solids entry (9) is advantageously avoided.
    The difficulty of heat transfer to a straw-water mixture is solved by first separating a low-viscosity fluid by means of a separator (2) which can be pumped well. This is preheated in the recuperator (21) and heated in the preheater cycle by preheater heat exchanger to about 70 ° C to 80 ° C. As Wärmequel¬le serves z. B. engine cooling water.
    In the circulation process or periodically, the valve is closed and taken over the Dosier¬ valve (42) from the preheating the necessary amount of recyclate / Separatorfluid removed and with Überdruck of z. B. pressed up to 6 bar in the prepared organic mass.
    According to the invention, the lignin-containing biomass must be heated to a temperature of preferably 75 ° C., particularly preferably 80 ° C., for at least a few seconds.
    Immediately after the introduction of solids, the biomass activator mixture has a mixing temperature below 70.degree. Thereafter, the heat exchanger is reheated to approx. 80 ° C. This triggers the microbiological reaction and lignin splitting begins.
    After splitting, mixture is optionally cooled, e.g. B. in countercurrent heat exchange. The temperature drops below 60 ° C and is fed to the fermenter. In the fermenter, the biomass composition is fed to the fermentation. Now the previously lignin-protected biomass components are unlocked.
    Depending on the input material (eg straw), this means an additional yield of up to 300% (up to 600 cubic meters per ton of dry substance) compared to the processes of the prior art.
    EXAMPLES (The reference numbers refer to FIG. 5) EXAMPLE 1 [00125] In repowering of existing plants, the repository initially still has high solids fractions. Digestate is removed from the repository (1) and fed to a separator (2).
    This separates the digestate into a solid fraction (51) with z. B. 25% OTS and a fluid content (52) of z. 4% OTS. The separator fluid is stored intermediately in the separator fluid container (3) and, if necessary, heated frost-protecting.
    The solid portion (51) is also stored and, if necessary, conveyed to the feed side to the solids mixer (8) to be mixed with the feedstock. The fluid portion (52) with z. B. 4% OTS is sucked from the storage container (3) by a pressure-generating pump (31) and compressed to a flow pressure of up to 5 bar.
    With some pressure drop, this low viscosity and chemically alkaline separator passes fluid (53) through a heat exchanger (21) where it receives heat from a heated counterflow (57). The countercurrent is the finished heated and activated feed mixture on the way to the fermenter (58).
    The preheated separator fluid is pressed into an inlet mixing chamber (82) and generates in this way in the circulation circulation (55) a system pressure of up to 4 bar. the addition is possible here only when the valve (43) is open. Optionally, in the circulation circuit (55) of the pre-heater, a buffer tank with separator (4) is incorporated, which contains a refillable storage element.
    The circulation circuit (55) is driven by a circulation pump (32), which is less directed at pressure build-up, but it is designed especially corrosion resistant and special temperature resistant. The pressure difference to be generated is that of the pressure loss in the circulation circuit through the heat exchangers (22) and the mixing chambers (82, 83, 84).
    The pre-heater (8) is designed as a tube heat exchanger. In countercurrent, engine cooling water is heated, which is taken from the biogas CHP. The heating is thus 100% renewable.
    The circulation circuit flows through an outlet mixing chamber (84), at which the faster is reduced, so that a dynamic pressure acts on the metering valve (42). When the engine valve (42) opens, heated separator fluid (55) may flow to the solids feed (9) at about 80 ° C or higher.
    On the way to the solids entry (9) is an injection for the activator (bionics fluid) from tank (6) and purified hot water, this opens into chamber (81).
    The feedstock entry via a solids mixer (8). This mixes fresh biomass with recycle (51) from the separator (2) and crushed straw as needed, and also adds a functionally very important biological component from the tank (7), the activator. The starting material is here also comminuted to a particle size / pin length less than 30 mm, preferably about 10 mm.
    The premixed feed is compressed in the solids feed device (9) and intimately mixed with the preheated separator fluid from chamber (81). In this case, the separator fluid is preferably the larger mass fraction and also has the higher specific heat. The biomass formulation (56) with a mixing temperature of z. B. below about 70 ° C.This biomass preparation (56) is mixed with activator but not yet fully activated. It is therefore heated further until activation and then cooled slightly in the recuperator. In front there it goes to the fermenter. EXAMPLE 2 In continuous operation, the biomass preparation from the system according to the invention is almost completely utilized in the fermenter. As a result, the organic solids content falls several to several months in the repository (1) to less than 4%. Now no separator (2) is required anymore. The final storage liquid can be used directly as a liquid feed (52). Example 3 [00136] As feedstock, z. B. mainly dry straw are used, for. B. weildieses incurred in a large agricultural business as waste. In this case, the straw must be chopped. The OTS content of straw is over 85%. For processing, an admixture of liquid must be carried out, e.g. B. fermenter liquid. However, this has increasingly high mineral content. Consequently, moreover, water is mixed into the feed preparation in order to prevent the mineral concentration in the fermenter and repository from becoming too high in the long term. EXAMPLE 4 Chicken meal as a feedstock has an oversupply of ammonium. Then, a precipitating agent is metered from a metering tank (5) into the separator (4) to precipitate ammonium fertilizer from the heated circulating liquid (55). In this way, metal ions and other components from the preheater cycle can also be precipitated. EXAMPLE 5 The biomass fluid circuit is to be rinsed. For this purpose, the inlet valve (43) is opened and the circulation valve (41) closed. The metering valve (42) is opened and the solids entry is bridged when needed or not (not shown). Then, the fluid carried by the pumps (31) and (32) flows through all the heat exchangers and cleans them. After the recuperator (21), the fluid can also be pumped back into the container (3) (not shown). EXAMPLE 6 A particular biomass requires particularly high activation at elevated temperatures. Then first the metering valve (42) is closed and the separator fluid (55) circulates through the heat exchanger (22) and heats up to 85%. Correspondingly, only a small amount of solid material is supplied and the result is an increased mixing temperature in the E-mix (56). This is further increased in the reheater (23). If necessary, the recuperator (21) could also be switched to heating mode in order to further increase the activation of the fluid (57). Reference sign reference list for FIG. 5 1 final storage container 2 separator 3 separator fluid container 4 separator 5 precipitator 6 bionics HAT tank 7 bionics LT tank 8 solids mixer 9 solids entry 21 recuperator heat exchanger 22 preheater heat exchanger 23 reheater heat exchanger
    31 pressure pump 4 bar 20-50 ° C
    32 Circulation pump 1 bar 70-90 ° C 41 Circulation valve in preheating circuit 42 Metering valve for solids entry 43 Inlet Valve for preheater 44 Overflow Valve from preheater in separator fluid 45 Drain valve from separator 51 Separator Material Solid Digest 52 Separator Fluid TS04 cold low viscosity 53 Separator fluid in Outer jacket warmed up
    54 Separator fluid through inlet valve 50 ° C
    55 Separator fluid TS04 in preheater circuit 80 ° C
    56 E-mix after addition of solids <70 ° C
    57 E-Mix TS12 after heating 80 ° C 58 E-Mix TS12 cooled 55 ° C to fermenter 91 Engine cooling water heats preheater 22 92 Engine cooling water heats reheater 23 93 Engine cooling water heats separator fluid 3 as required 94 Engine cooling water heats Bionik HT Tank 6 95 Engine cooling water heats solids in requirement
    The mode of operation of the BMT system is preferably clocked. A. Inlet stroke and at the same time discharge from the circulation into admixture B. Heating cycle in circulation and at the same time reheating in heat exchanger 23 and cooling in WT 21. Then again A.
    权利要求:
    Claims (8)
    [1]
    Claims 1. A device for producing a biomass preparation, comprising: - a device for introducing a difficult-to-open biological starting material (50), wherein the difficult-to-open biological starting material ligninhaltig, - an activator (42, 70) for digesting the starting material, when exceeded a temperature TA is activated, with TA &gt; 55 ° C, wherein the activator thermophilic microbes in ei¬ner concentration of more than 1 million per milliliter, which are activated from the temperature TA, and - a device (21) for the thermal activation of a combination of reactant and Akti¬vator.
    [2]
    The device of claim 1, further comprising: means (9) for contacting the reactant with the activator.
    [3]
    3. Device according to claim 1 or 2, wherein the means for thermal activation (21) comprises a heat exchanger or a heater.
    [4]
    4. Device according to one of claims 1 to 3, further comprising: - a mixing device (8) for educts.
    [5]
    5. Device according to one of claims 1 to 4, further comprising: - a metering device (41) for a metered addition of the activator (42).
    [6]
    6. Device according to one of claims 1 to 5, further comprising: - a mixing device (9) for mixing the starting material from different solid, Breiförmi¬gen or liquid educts.
    [7]
    7. Apparatus according to claim 3, wherein the heating means is heated by chemical energy or reaction heat or electromagnetic energy or radiation.
    [8]
    8. The device according to one of claims 1 to 7, further comprising: - a means for heat recovery (23). For this 3 sheets of drawings
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    同族专利:
    公开号 | 公开日
    DE102014003159A1|2015-09-03|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    CA1084762A|1976-04-26|1980-09-02|Thomas L. Coulthard|Thermophilic aerobic digestion process for producing animal nutrients and other digested products|
    WO2008000809A1|2006-06-30|2008-01-03|Biogasol Ipr Aps|Production of fermentation products in biofilm reactors using microorganisms immobilised on sterilised granular sludge|
    EP1978086A1|2007-03-13|2008-10-08|Stirl Anlagentechnik GmbH|Method for hybrid decomposition of biomass containing lignocelluloses|
    US20110306089A1|2010-02-12|2011-12-15|Sowers Kevin R|Thermophilic methanogenic consortium for conversion of cellulosic biomass to bioenergy|
    DE3138309A1|1981-09-25|1983-04-14|Walter 8530 Neustadt Feilhauer|Biological digestion of lignin-containing substances|
    DE3341691A1|1983-11-18|1985-05-30|Walter 8531 Schauerheim Feilhauer|Process and apparatus for the anaerobic treatment of organic substances|
    ZA957645B|1994-09-13|1996-10-14|Innoval Management Ltd|A method for production of ethyl alcohol|
    DE19858187C5|1998-03-16|2006-05-18|Eisenmann Maschinenbau Gmbh & Co. Kg|Method and apparatus for reducing the organic content of an expandable substrate|
    DE102005030895A1|2004-07-23|2006-03-16|Eckard, Horst K.|Apparatus for breaking up biological material in dispersion comprises tank, around which ultrasound generators are mounted which are focused on its center|
    US8895290B2|2008-10-17|2014-11-25|Maxbiogas Gmbh|Method for digesting a biomass comprising lignin together with cellulose and/or hemicellulose|
    DE102011113646B3|2011-09-19|2013-01-03|Prüf- und Forschungsinstitut Pirmasens e.V.|Apparatus and method for the hydrothermal digestion of dried, woody lignocellulose-containing biomasses|
    DE102011118067A1|2011-11-09|2013-05-16|Obermeier - Widmann GbR |Treatment process of biomass with the addition of at least one activator|DE102015221919A1|2015-11-09|2017-05-11|Koenig & Bauer Ag|Winding device for web-shaped material and method for drawing at least one material web in at least one winding device|
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    申请号 | 申请日 | 专利标题
    DE102014003159.4A|DE102014003159A1|2014-03-03|2014-03-03|Apparatus and method for producing a biomass preparation, in particular from feedstocks with a high lignin content|
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