DE102014011479A1 - New process for the fermentation of biogenic energy sources - Google Patents

Abstract

The invention relates to a process for the anaerobic fermentation of biomass and its implementation in a plant with the aim of parameter-controlled generation of a liquid phase which is enriched with intermediates of anaerobic degradation for the utilization of existing technical equipment for methane production (digestion of sewage treatment plants, biogas plants) or material use. The procedure is strictly anaerobic and works batchwise. According to the invention, only the processes of hydrolysis and acidogenesis take place here, which is realized by a pH regulation and the strict separation of the process liquids and the populations contained therein. So there is no methane but still a biogas that mainly consists of H2, CO2, H2S and NH3. This is reacted in a container reactor for hydrogenotrophic methanogenesis. According to the invention, the control of the fermentation time - ie the formation of intermediate products - takes place via the measurement of the biogas formation and the consumption of the alkaline additive for the regulation of the pH. By combining N-stressed with C-emphasized starting materials, the consumption of the alkaline additive can be minimized according to the invention. According to the invention, the method is technically implemented in a modular system in container construction. The input materials are delivered by means of special transport containers and, together with the containers, placed in modular garages where the biomass is converted into intermediate products of anaerobic degradation by means of controlled hydrolysis and acidogenesis. With the help of a temporary storage tank containing process liquid, the containers are percolated, flooded and returned cyclically, so that the forming intermediate products accumulate from the degradation of the biomass in the temporary storage tanks. By contrast, liquid feedstocks can be introduced directly into the intermediate storage tanks and the latter can additionally also be operated as stirred tank reactors having the same objective (hydrolysis / acidogenesis). Since the buffer tanks are provided with a pH control, the biomass is largely degraded during short fermentation times and there are no product inhibitions. Subsequently, with the thus produced, high-energy liquid phase further optimization steps (nutrient ratios, inhibitors) are operated before z. B. is used for the utilization of external bioreactors for methane formation according to the prior art. However, these are not part of the invention.

Description

Basic idea of the system

Starting point / background

Method and plant (modular system) for multi-stage fermentation of solid or liquid biogenic energy sources for the production of energy and raw materials Existing technologies and processes for single or multi-stage methane gas production are based on the aerobic or anaerobic decomposition of biomass Rule just for remainder disposal. These include comparable systems; z. B. the Rohn hydrolysis, or biogas plants of Fa Gicon,
It was considered among others. the patents DE 10 2010 0287 07 A1 , such as DE 11 2006 001 877 A5 , or WO002007012328A1 ,

• • Ferner gibt es im Grunde keine technischen Standards oder Modularisierungen, die es ermöglichen würden, die Anlagen wirtschaftlich modular zu bauen, anstelle jede Einzelne, wie es bislang geschieht, individuell zu planen und zu erstellen.
• • Dazu gibt es keine fertigen Steuerungs- und Meßeinrichtungsmodule (Sensorik), die mittels automatischer Überwachung und Regulation diese Prozesse optimal steuern.
• • In den diversen Verfahren gibt es ferner Grundprobleme der gleichmäßigen Verteilung der Einsatzstoffe/bzw. Homogenenisierung mittels Mischtechnologien z. B. durch Rührwerke,– die Homogenität der Biomasse während der Zersetzung bzw. Perkolation ist oft nicht gewährleistet
• • bis hin zu Be and Entlade-Problemen ganz praktischer Natur, indem es heute sehr umständlich ist, solche Anlagen mit Biomasse zu bestücken und ständig auch kontinuierlich Reststoffe nach Zersetzung zu beseitigen. (Radlader etc.)
• • Im Bereich der Perkolation gibt es bislang keine Vorrichtungen oder Verfahren, die hier die Transport und Lagerungstechnik mit dem eigentlichen Zersetzungsprozess (Reaktor) in direkte funktionelle Verbindung bringen., (Wechselcontainer)
• • Im Bereich der Methanogenese gibt es einen Syntheseprozess in dem CO₂ nicht nur herausgereinigt sondern zusammen mit anfallendem Wasserstoff eine aktive Synthese zu Methangas erreicht wird unter Verwendung von CO₂ und H₂.
• • Im Bereich von laufenden Kläranlagen gibt es selten Kombinationen mit sinnvoll angekoppelten Biogasanlagen zur Abdeckung des Energiebedarfs der Reaktoren der Kläranlagen selbst.
• • Es wurden keine anderen Wettbewerber gefunden, welche eine Technologie-Kombination als Einzelsystem modular oder als Aufrüstungsmaßnahme für Kläranlagen bereitstellt.

Apart from the rising costs of biomass, this power generation technology is currently stagnating due to high costs and high production costs as well as energy storage and distribution issues.

• • Furthermore, there are basically no technical standards or modularisations that would make it possible to construct the systems in an economically modular way, instead of individually planning and creating each individual as has been done so far.
• • There are no finished control and measuring device modules (sensors) that optimally control these processes by means of automatic monitoring and regulation.
• • In the various procedures, there are also basic problems of uniform distribution of feedstocks / or. Homogenization by means of mixed technologies z. B. by stirrers, - the homogeneity of the biomass during decomposition or percolation is often not guaranteed
• • up to loading and unloading problems of a very practical nature, in that today it is very cumbersome to equip such plants with biomass and to constantly eliminate residues after decomposition. (Wheel loader etc.)
• • In the field of percolation, there are no devices or processes that bring the transport and storage technology into direct functional connection with the actual decomposition process (reactor)., (Exchange container)
• • In the field of methanogenesis, there is a synthesis process in which CO _{2 is} not only purified but together with accumulating hydrogen, an active synthesis to methane gas is achieved using CO ₂ and H ₂ .
• • In the field of running sewage treatment plants there are rarely any combinations with sensibly linked biogas plants to cover the energy requirements of the reactors of the sewage treatment plants themselves.
• • No other competitors were found that provided a combination of technologies as a single system modular or as an upgrade to wastewater treatment plants.

According to the invention, it is an innovative technique of "multi-stage hydrolysis and acidogenesis stage" for which there is no comparable system on the market which solves the aforementioned problems in a new way. The solution is to create a pre-treatment system for biomass, which is suitable both for use in municipal wastewater treatment plants, as well as for biogas plants and produces a high-energy liquid phase enriched with intermediate products of anaerobic degradation. This is realized or supported by a mobile modular design.

• – Senkung der Energiekosten um mind. 25%
• – volle Auslastung der BHKW Leistung und des Faulraumvolumens
• – Minimierung der Entsorgungskosten durch zusätzliche Behandlung von vorhandenen Abfällen (Rechengut, Schlämme)
• – Ausbau kleiner Kläranlagen mit anaerober Stufe nun wirtschaftlich sinnvoll

The economic goals in the connection of the system with sewage treatment plants are:

• - Lower energy costs by at least 25%
• - full utilization of CHP capacity and the volume of septic tanks
• - Minimization of disposal costs through additional treatment of existing waste (screenings, sludges)
• - Expansion of small sewage treatment plants with anaerobic stage now makes economic sense

Thus, an increase in energy efficiency in municipal sewage treatment plants to energy self-sufficiency is achieved. Wastewater treatment plants are buildings with high investment costs. They are predominantly built with subsidies and are therefore subject to the mechanisms of action of conditions and provisions, the z. B. reuse, construction and decommissioning etc. at least. Wastewater treatment plants currently generate about 30% of household energy costs.

• – Senkung des Eigenverbrauches durch spezifische Lösungen, zugeschnitten auf die Bedingungen der KA
• – Ausschöpfung der Potentiale der Stromerzeugung aus Inhaltsstoffen des Klärprozesses
• – Einsatz geeigneter Co-Fermente aus dem Potential von Indirekteinleitern (z. B. Fettabscheider) bzw. kommunalen Zugriff

Up to 60% of the energy costs of wastewater treatment are caused by ventilation costs. Overcoming the imbalances between energy consumption and energy production in sewage treatment plants is done by

• - Reduction of self-consumption through specific solutions, tailored to the conditions of the KA
• - Exploitation of the potentials of power generation from ingredients of the clarification process
• - Use of suitable co-ferments from the potential of indirect dischargers (eg grease separators) or municipal access

• 1. De-Ammonifikation mit Scheibentauchkörpern
• 2. Entwässerungsverfahren mit Bucherpresse und Strovit-Fällung (Phosphorrückgewinnung)
• 3. Einsatz von Membranklärverfahren
• 4. Einsatz von Hochlastfaulung und Nachvergärung
• 5. Kaskadenbiologie mit Restdenitrifikation in Filteranlagen und SRC Technik

Conventional technical solutions that are used in sewage treatment plants and represent the state of the art:

• 1. De-ammonification with disc submersibles
• 2. Method of dewatering and stoving precipitation (phosphorus recovery)
• 3. Use of membrane clarification process
• 4. Use of high-load digestion and post-fermentation
• 5. Cascade biology with residual denitrification in filter systems and SRC technology

According to the industry, only 35% of wastewater treatment plants in Germany use co-fermentation. This is attributed to the lack of availability of co-fermenters and their lack of business management. It is also stated that biomass is not permanently available due to the competition of agricultural biogas plants and can not be reconciled with the process engineering of the sewage treatment plant due to the nitrogen loads from the biomass, since the increased yield of gas would be offset by the increased expenditures for the removal of nitrogen. Experiences and comparisons of decomposition rates of the organic substance from the digestion process show that with the help of biological process improvements the sewage sludge quantity can be lowered significantly and the power / heat yield can be increased. Digestion methods and pretreatments of individual sewage sludge substrates have been described e.g. Part tested in the practice of sewage gas plants, the results are not generalizable. From the state of the art, no methods are recognizable which offer solutions for sewage sludge disposal in the value chain of sewage treatment plants / municipalities with respect to new regulation in business terms.

• – jeder Faulturm ist ein individuelles Bauwerk, es gibt im Wesentlichen. keine Standardisierung
• – die verfahrenstechnische Vielfalt des Vergärungsprozesses ist gering, seit Jahren gibt es keine durchgreifenden Innovationen durch fehlende Motivation und Wettbewerb.
• – die technischen Entwicklungen z. B. Pumpen, Pressen, Zentrifugen, Filter usw. finden überwiegend ohne Beachtung des Primates der biologischen Prozesse statt
• – Veränderungen der Wichtigkeit von Stromkosten und Betriebswirtschaftlichkeit bildet positive Rahmenbedingungen für die Überwindung dieser Entwicklungen
• – bei der energetischen Bewertung werden Kläranlagen und die einzelnen ineinander greifenden Prozesse nicht ganzheitlich gesehen
• – Konzepte für die stabile, ganzjährige Zuführung von geeigneten Co-Substraten. Aufbereitung von Biomasse, Herstellung von Flüssigperkolaten mit aufkonzentrierten organischen Säuren aus Substraten aus dem Zugriff der Kommunen
• – Lösungen zur Stickstoffabtrennung im nicht mit der KA verbundenen Perkolatkreislauf
• – verfahrenstechnische Lösungen zum Einsatz in KA der Gruppe 1–3, um dort anfallendes organisches Potential energetisch für Klärgasanlagen zu erschließen
• – verfahrenstechnische Lösungen für die Aufschlussverbesserung von Primärschlamm und die Zuführung von organischer Restbestandteile aus Überschussschlamm
• – verfahrenstechnische Lösungen durch. Veränderungen in der Zusammensetzung der organischer Säuren, evtl. mittels externer Zuschlagstoffe um für die jeweiligen Bedürfnisse der Kläranlage ”passende Co-Fermente” anzubieten
• – Einführung vereinfachter und standardisierter Fermenter und Peripherieausstattung, Heizung, Rührwerke, Pumpen, Zerkleinerer usw. für Bauformen zum Einsatz in 25 000 bis 100 000 EW-Kläranlagen
• – vereinfachte Prozessanalytik und Überwachungs- und Steuerungstechnik aus zentralen Leitwarten für diese Prototypanlagen

In summary, it can be stated:

• - Every trough tower is an individual construction, there are essentially. no standardization
• - The procedural diversity of the fermentation process is low, for years there has been no radical innovation due to lack of motivation and competition.
• - the technical developments z. As pumps, presses, centrifuges, filters, etc. take place predominantly without regard to the primate of the biological processes
• - Changes in the importance of electricity costs and business management form a positive framework for overcoming these developments
• - In the energy assessment, sewage treatment plants and the individual interlocking processes are not seen as integral
• - Concepts for the stable, year-round delivery of suitable co-substrates. Preparation of biomass, production of liquid percolates with concentrated organic acids from substrates from municipal access
• - Solutions for nitrogen separation in non-KA Perkolatkreislauf connected
• - Process engineering solutions for use in KA of Group 1-3, in order to exploit the organic potential arising there for the energetic use of sewage gas plants
• - Process engineering solutions for the digestion improvement of primary sludge and the supply of organic residues from excess sludge
• - procedural solutions by. Changes in the composition of the organic acids, possibly by means of external additives to offer for the particular needs of the treatment plant "suitable co-ferments"
• - Introduction of simplified and standardized fermenters and peripheral equipment, heating, agitators, pumps, shredders, etc., for types for use in 25 000 to 100 000 domestic sewage treatment plants
• - Simplified process analytics and monitoring and control technology from central control rooms for these prototype plants

• – Verringerung der Verweilzeit um bis zu 50% von 21–28 Tagen auf 7–14 Tagen
• – Erhöhung des Gasertrages um bis zu 30% durch höheren Abbaugrad
• – Steigerung der BHKW Auslastung >= 8000 h
• – Höhere Prozessstabilität
• – keine externe Beschickung mit Radlader spart erhebliche Personalkosten ein

The solution consists in a device for use in a co-fermentation process suitable for sewage gas plants, also within standardized plants for use in 25 000 to 100 000 EW sewage treatment plants. Further development of solid-state fermentation means:

• - Reduction of residence time by up to 50% from 21-28 days to 7-14 days
• - Increase of gas yield by up to 30% due to higher degree of degradation
• - Increase in CHP utilization> = 8000 h
• - Higher process stability
• - no external load with wheel loader saves considerable personnel costs

The system offers the highest possible flexibility - because both stackable biomass and liquid substrates are used - renewable raw materials as well as the usual waste streams (eg farmyard manure, landscape care material or biowaste).

• – Aufgrund einer fehlenden Durchmischung, mech. Aufschlusses und ungleichmäßiger Perkolatverfügbarkeit ergibt sich ein insgesamt ungleichmäßig ablaufender Gärprozess
• – Fehlgärungen sind die Folge durch partielle Akkumulation von organischen Säuren
• – Perkolationsführung bei vielen Anlagen sehr unterschiedlich und oft vernachlässigt, aber eine der wichtigsten prozesstechnischen Stellschrauben
• – Perkolatdurchfluss durch Haufwerk nicht optimiert, kann aber durch bestimmte Substrat-kombinationen und Drainagesysteme maßgeblich verbessert werden
• – niedrige Substratnutzung und schlechter Abbaugrad senken Wirtschaftlichkeit beträchtlich und verursachen Geruchsbelästigungen
• – schwierige Weiterverarbeitung der Gärreste und Geruchsprobleme durch schlecht vergorenes Material
• – spezifische Biogasbildung von Trockenfermentationsanlagen liegt teilweise 30% unter dem von Nassfermentationsanlagen
• – Perkolateigenschaften für anaeroben Abbau oft nicht effektiv; führt zu Problemen bis hin zum Verstopfungen des Perkolationssystems und Totalausfall
• – Ablagerungen durch z. B. MAP/Schwefelablagerungen verursachen teils massive technische Probleme
• – herkömmlicher Einsatz von Hilfsstoffen (z. B. Spurenelemente) ungelöst, da diese mit dem Haufwerk ausgetragen werden, sodass deren Einsatz zu teuer wird

The following problems have been recognized in recent years with regard to the process of garage fermentation with percolation and are also solved by the system:

• - Due to a lack of mixing, mech. Digestive and uneven percolate availability results in an overall unevenly occurring fermentation process
• - Mild fermentation is the result of partial accumulation of organic acids
• - Percolation control in many systems very different and often neglected, but one of the most important procedural set screws
• - Percolate flow through debris has not been optimized, but can be significantly improved by certain substrate combinations and drainage systems
• - Low substrate utilization and poorer degrading efficiency significantly reduce efficiency and cause odor nuisance
• - Difficult further processing of digestate and odor problems by poorly fermented material
• - Specific biogas production of dry fermentation plants is partly 30% below that of wet fermentation plants
• - percolate properties for anaerobic degradation often not effective; leads to problems up to clogging of the percolation system and total failure
• - deposits by z. B. MAP / sulfur deposits cause some massive technical problems
• - conventional use of excipients (eg trace elements) unresolved, since these are discharged with the debris, so that their use is too expensive

The technology provides is also a basic technology for advanced low-tec biorefineries. One of the system's core ideas is to collect biogenic waste decentrally with a swap-body system, transport it to the plant and bring it directly into the garage fermenter. The interchangeable container initially serves to collect and transport the substrates to the site of the plant - then all the technical components for the implementation of the process are connected, with the aim of producing an organic acid-enriched liquid phase. This liquid phase then serves, after further optimization, to utilize the capacities or to expand the methane production on the sewage treatment plant.

To realize this objective, the plant is constructed as wet and garage fermentation. With regard to garage fermentation technology, the known technical disadvantages are eliminated. Due to the much more effective degradation processes, it is now possible to minimize the required reactor volumes to container size and still achieve a high throughput. From a process point of view, the anaerobic processes used are therefore advanced hydrolysis-acidogenesis precursor systems in combination with the garage fermentation technology. The aim is to produce a high-energy liquid phase from stackable biomass for further processing. This offers a variety of synergies and opportunities for energetic use.

The technology can also be used as a standalone biogas system, but it is specially designed to take into account the specificities of municipal wastewater treatment plants, as there is currently enormous market potential. The container concept enables maximum mobility and integrates essential, process-technical innovations into a compact and modular system concept.

The system is modular and can be dismantled to ensure maximum flexibility. Thus, the system also includes an automated analysis station, which automatically samples multiple reactors, i.a. a. with the goal that the high-energy liquid phase produced in the system can be automatically dosed into the methane-forming process stages as needed. Crucial here is that this liquid phase is lower in terms of the necessary residence time to achieve an optimal degree of degradation, than that of the other input materials of the digestion stages. Furthermore, all parameters of the liquid phase can be influenced such. The trace element content, the C: N: P: S ratio and the nitrogen and sulfur loadings. In this way co-fermentation can be decisively optimized and adapted to the respective conditions.

The analysis system is integrated into a mobile, central pumping and analysis station, which serves as an interface for all media transport, dosing and measuring tasks. Here, the entire media transport of the fermenter system is controlled and thus results in this interface, the possibility to optimize the process liquids - on the one hand before recirculation in the garage reactors, on the other hand before feeding the digestion stages.

When feeding the digestion towers not only the measured values are decisive, but also B. also the micro and macronutrient ratio. Accordingly, the digestion stages can be optimized by using the overall system to high-performance fermenters, since best conditions are created with regard to the process parameters.

Description of how it works

1. Substrate procurement

The input materials (eg organic waste, landscape care material, organic fraction residual waste, etc.) are collected by the producer in interchangeable containers (A). Once this is filled and can be removed, it is replaced by an empty one.

2. Loading the system

The full transport containers are placed in the reactor arrays (B) and all module components as well as the percolation system connected. The fermentation process begins after the garage doors have been fired and the percolation has started.

3. acidogenic process stage

The withdrawn process water from the garage reactors is in one of the process water storage (C) promoted and kept there by alkaline addition of a memory (D) or by adjustment of the input mixture between pH 5.5-6,0. This is the optimal range for the aciodogenic phase in the breakdown of carbohydrates and can be adjusted according to the input. The pH in the garages decreases theoretically continuously and is z. B. kept constant by the alkaline additive and the circulation. This results in very short degradation times of about 4-10 days to about 80% of the organic fraction have been completely converted to organic acids. In addition, the processes here are optimized with regard to the nutrient supply with micro- and macronutrients, as well as by controlling the dissolved NH ₃ and H ₂ S contents in the liquid phase. Thus, the liquid phase can be prepared in each case for renewed percolation in the garages or for feeding into the digestion stages.

4. Reaction to methane

When the acidification is complete and the process water storage tank has its optimal concentration of org. Acids reached, this is switched and fed from now on only the digestion stages or methane levels (E). The other process water storage is then used during this time to percolate the garage reactors. The result is a change cycle, so that each store provides the garages with process water, the other hand, the liquid phase - enriched with organic acids - transported to the methane production in the digester. However, this does not happen directly because previously the liquid phase in the memory is optimized in terms of important parameters.

5. Methane formation in the garages as the last step in the process

The resulting, liquid digestate from the digester can be transported after the acidification phase in the container of the garage reactors, there to raise the degree of degradation further. During this time, methane is also extracted from the garage reactors. However, the garage reactors then have no contact with the process water storage and so a strict spatial process separation is guaranteed.

Basically, there are several scenarios for using the system at municipal wastewater treatment plants or biogas plants. The most important approaches will now be presented, which also describes the market potential. In most cases, the volume of septic tanks or CHPs is underutilized in sewage treatment plants. Co-fermentation is generally suitable here, especially if it is foreseeable that this underutilization will persist in the long term. If only the CHP is underutilized, consideration may be given to extending the volume of the septic tank, taking into account the future development and simultaneous use of the system. Thus, a step towards energy self-sufficiency can be made in order to significantly increase plant economy.

Covering the own electricity demand with methane power generation is an essential means of reducing the costs on municipal sewage treatment plants and is a promising starting point for the use of the system. Most plants only manage to cover around 40% -50% of their own electricity needs without the use of co-fermentation. With the use of technology, it will now be possible to cover up to 100% initially and even beyond, to feed surplus produced into the grid. As a result, sewage treatment plants become energy suppliers and additionally utilize the municipal and industrial biogenic waste streams. Of course, this requires appropriate amounts of waste. Some smaller wastewater treatment plants do not have an anaerobic digesters (digestion towers) for methane extraction. This depends u. a. with the size of the catchment area. Generally, however, anaerobic post-treatment or fermentation makes energy sense, in particular in order to reduce the own power requirement.

An anaerobic process line could also be constructed for these plants, dimensioned to take into account future regional developments and the use of the system - to achieve the same cost structure benefits.

Procedure / Overview

Process description:

• 1) Exchange containers are filled in exchange and transported to the plant;
• 2) Swap bodies have a double bottom (sieve bottom) and have a transport cover
• 3) When the filled container is delivered, the transport lid is replaced with a gas-tight special lid
• 4) This is a distribution system for sprinkling the garage with process water from the store
• 5) The media lines are connected directly to the container
• 6) Garage door is closed
• 7) The container is flooded from below and above with process water and after a defined time the process water is transferred back to a storage tank
• 8) Organic acids are formed by hydrolysis / acidogenesis
• 9) In the process water tank, the process water is regulated with regard to the pH value
• 10) This is done either by alkaline addition
• 11) or by mixing the process liquids in the storages
• 12) or by simultaneous use of a C-emphasized and an N-stressed substrate, so that alkaline additive can be completely substituted in the best case
• 13) the process water tanks alternately feed either the garages with process water (hydrolysis / acidogenesis) or the digestion stages to form methane
• 14) so that one store will do the percolation for all the containers, while the other will charge to the methane stage, then bills of exchange
• 15) The hydrolysis gas formed is injected from all fermenters into a special container by means of distributors, so that CO2 and H2 are converted to methane (hydrogenotrophic methanogenesis); The methane produced is fed to the methane stages
• 16) The fermentation time in the hydrolysis / acidogenesis is determined by the formation of hydrolysis gas; acidification also stagnates in stagnation
• 17) After degradation of the biomass to organic acids and other dissolved substances, the liquid phase is transferred to the storage; then a digestion by flooding of the container is effected with digested sludge, whereby these are decoupled from the memories; the methane is transferred to the digestion stages
• 18) Subsequently, the swap body is removed from the garage and further processed externally; This is done by connecting other components outside the garage (drying / composting)

Main process features:

• 1) pH control - Control of the pH value by mixing the hydrolyzate - So that constantly pH 5.5-6.0 is present in garages and in any case above pH 5.0 - How to avoid end product inhibition Acidogenesis - Requires 2 feedstocks: highly acidic and protein-enhanced substrate - Otherwise pH control via alk. Additions because special case cross-flow but substitution
• 2) Compensation C: N ratio over inoculation in the initial phase - deficiency at N detected in the initial phase (corn silage) - Addition N improves degradation
• 3) control of cycles via stagnation hydrolysis gas formation / consumption alkaline additive; correlates with optimum acid formation
• 4) Change cycle of percolate storage: Feeding digester / loading garages
• 5) Optimization steps N: S as a treatment step before methanation
• 6) after acid formation in garage digested sludge in garage and contact to process water storage interrupted 4 strict spatial separation of the anaerobic processes

Bioraffineriefunktion:

• - sanitation biomass (temp.)
• - Inoculation with desired microorganisms from separate storage, so that organisms prevail and form special products
• - pH control and other operating parameters
• - thus targeted production of z. As lactic acid, butyric acid, propionic acid

Technical innovations

• 1) Multifunction interchangeable container (transport, fermentation, drying, composting)
• 2) automated FOS / TAC system
• 3) Hydrolysis from below and percolation from above (damming-deflation rules etc ...)
• 4) Mobile Garage
• 5) Solid and Liquid (process as percolation process and in a stirred tank for non-percolable feedstocks)
• 6) Hydrogen and CO2 are converted into methane containers for injection

Special procedures

• 1) no loading by means of wheel loader, but special interchangeable containers are used, which are used as a collection container and at the same time as a fermenter, so no reloading is necessary
• 2) the exchange containers serve as transport containers, get another attachment in the plant and be used directly as Aufschwimmfermenter
• 3) in the process water storage a pH between 5.0 and 5.5 is maintained by alkaline addition; Furthermore, that the additive is substituted by combining strongly acidifying substrates and basic to neutral - due
• 4) the protein or nitrogen content; then mixing the process water streams in stores to balance the pH and nutrients
• 5) by controlling the pH end-product inhibition is avoided
• 6) by selecting a nitrogen / proteinaceous substrate, an initial ammonium undersupply is avoided
• 6) preferably do not incubate any methanogenic archaea in the hydrolyzate reservoir, thus producing an adapted process water and strict separation of the media; Remaining part of the cultivated process water as inoculum for next cycle
• 7), in particular a C-stressed, as well as an N-stressed substrate are preferably used quantitatively so that the pH does not move below 5.0 and not above 5.5 during acidogenesis - without external control
• 8) the pH of the input mixture and substrate characteristics are adjusted to achieve maximum throughput and degradation
• 9) in the reactors, process water is cyclically dammed up from below and transferred back into the reservoir for controlling the ph; thus avoiding inhomogeneous zones and better removal of the products
• 10) at least 2 memories are present, one each realizing the supply of the reactors with process water, so that there concentrate the acids; the other, however, transfers its concentrated cargo to a methane / digestion tower during this time; then change
• 11) after stagnation of acid formation in reactors they are decoupled from the reservoirs and flooded with digested sludge to increase degree of degradation; then methane formation in garages; then change container out of the plant to externally carry out further steps (drying, composting) with interchangeable container connections
• 12) also liquid and pumpable substrates in a fermenter or storage without double bottom are mixed with pump; pH control right here until acid formation stagnates; then transfer of all cargo to methane; up to 60 kg otS / m3 input concentration (7-day batch process); Optimal 30 kg oTS / m3
• 13) that no air enters the reactors and they are strictly anaerobic; any resulting hydrolysis gas may be purified and converted to a methane stage for hydrogenotrophic methanogenesis; Utilization of the energetic potential of the hydrolysis gas
• 14) the acids can be separated - in the process water reservoirs to substitute pH control and obtain biorefinery products (acid mixtures); Use Inoklum for the targeted production of acids
• 15) the system is completely built in containers and is modular
• 16) the process water before being fed in methane stage to C: N: P: S optimize trace element supply (temperature / additive)
• 17) the control of the fermentation time is done by means of hydrolysis gas formation; this stagnates as soon as acid formation stagnates; then decoupling from memory
• 18) was specially developed for wastewater treatment plants for the utilization of digestion towers
• 19) The reservoirs can also be used as reactors for the acidification of non-percolatable substrates - depending on the available substrates; while batchhydrolye with up to 60 kg oTs / m3; Residence time approx. 7 days; then transfer of all cargo to digester or previous separation

Legend Fig. 1:

• A)

  returnable container

  B)

  mobile garage (gas-tight)

  C)

  Garage door (gas-tight lockable)

  D)

  Attachment lid with distributor system and sieve bottom against floating layers

  e)

  heating system

  F)

  transport cover

  G)

  Sieve bottom of the removable container with reservoir

  H)

  Gas meter (hydrolysis gas)

  J)

  Distribution system for gases

  K)

  Reactor for hydrogenotrophic methanogenesis

  L)

  Media line to the next store (for mixing operations)

  M)

  Motor with stirrer

  N)

  pH controller with dosing pump

  P)

  Storage container trace elements

  Q)

  Storage tank basic additive

  R)

  Media line to storage (for mixing operations)

  S)

  external existing methane level / digester stage

  SP)

  Storage / process water / Hydrolysatspeicher / percolate / fermenter

  V1..V18)

  Valve

  P1..P12)

  pump

QUOTES INCLUDE IN THE DESCRIPTION

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Cited patent literature

• DE 102010028707 A1 [0001]
• DE 112006001877 A5 [0001]
• WO 002007012328 A1 [0001]

Claims (12)

Procedure ( 1 ) for the fermentation of solid or liquid biogenic feedstocks with the aim of the effective conversion of the biomass by parameter-controlled, anaerobic degradation by hydrolysis, acidogenesis, aceogenesis towards intermediate products of anaerobic degradation for further use A method according to claim 1, characterized in that the technical implementation takes place in the form of a mobile and modular container system, by means of the combination of container & garage reactors (A, B) with cyclic flooding and percolation (D) and downstream hydrolyzate storage (SP) for reciprocal alternating feed (Loading and unloading) either the fermentation garages (A, B) for inoculation or further transport of the concentrated hydrolyzate from the storage (SP) with the aim of material or energetic use z. b in existing state-of-the-art bioreactors (S) Process according to claims 1-2, characterized in that, when sufficient amounts of H ₂ and CO _{2 are produced} in the fermentation stages (B, SP), this hydrolysis gas is passed to a methane gas formation by means of hydrogenotrophic methanogenesis in a suitable reactor (K). A method according to claim 1-3, characterized in that a more efficient anaerobic degradation of highly hydrous and stackable biomass is possible in modular fermentation garages (B) with interchangeable containers (A) and / or hydrolyzate (SP), towards organic acids and other intermediate products of anaerobic degradation, which concentrate first in the liquid phase on the hydrolyzate (SP) and then returned for further use or to the also alternately operating fermentation containers (B) in a defined controlled cycle for inoculation, there to intermediates from the Hydrolysis or the local acidogenic process by means of the new flocculation process with percolation (D) or in the stirred tank principle to produce, or for the regulation of Acidogenese / hydrolysis in general with respect to nutrient ratios, buffer systems and operating parameters; with the result, the accelerated and controlled optimized decomposition and acidification of biomass with a total shortened fermentation time for subsequent methanogenesis or optional generation of further intermediate products with raw material value (biorefinery), both for energetic support and efficiency increase or co-fermentation of mostly single-stage bioreactors or digestion stages or for immediate material recycling (energy / raw material value), and additionally the re-use of the organic residual digested sludge from the bioreactor (S) after decoupling from the buffers (SF) as the last step of the first fermentation stage itself (A, B), ( 1 ) Method according to claims 1-4, characterized in that - the plant ( 1 ) operates in a defined controlled alternating rhythm in which the process water is alternately charged between percolation stores and the fermentation garages for controlled and enhanced intermediate formation and concentration of the intermediates in the store (SF), in which in the cyclical course (1-12 days change cycle) a group of fermentation garages (B) / exchange container (A) filled with biomass, then the inoculation with desired microorganisms from separate storage (SF), so that organisms prevail and then flooded cyclically from below / top with hydrolyzate from one of the two hydrolyzate storage (SF) (Flooding hydrolysis below, further percolation from the top) while the other memory belonging to the group then exclusively gives off the concentrated intermediates for further use, e.g. b in external methane stages (S) which each two memory for the supply of a group of fermentation garages are responsible for process water and these cyclically alternately in their function (concentration of the intermediates in the liquid phase by percolation and flooding of garages or removal of intermediates) what also fitted in the overall rhythm so happens that the fermentation container (B) in a possible methane gas phase (by introducing, for example, digested sludge as the last step of the process) of the other cycles (eg product formation by hydrolysis / acidogenesis) then completely spatially Separate and work equally anaerobically (decoupling of Hydrolyzatspeichern and inoculation with methanogenic populations for the implementation of remaining intermediates in the heap of the fermentation stage (B). A method according to claim 1-5, characterized in that there is a defined control for the overall process, (change cycle between the at least 2 percolation storage of a group and the supply of percolation reactors / garages or fermenters) (B) always at least one hydrolyzate each store (SP), (delivery phase), the supply of all of the group associated fermentation container in the garages takes over (process water supply / sprinkling), while the second or more hydrolyzate memory (SP), (absorption phase) the concentrated hydrolyzate from the last cycle in the reactors for methanogenesis (S) fed, while the hydrolyzate storage (SP) in turn alternate and the control of the cycles of the system, first through the regulation of the pH and the consumption of additive is done to shorten the fermentation time (avoiding end product inhibition) while continuing by amipitation in the initial phase, a compensation of the C: N ratio (Sp1, 2) so as to prevent nitrogen deficiency in the initial phase, then at controlled pH by targeted mixing of the hydrolyzate or by additive addition, the process of intermediate formation takes place at a constant value between pH 5.0-6.5, so a To prevent end product inhibition of acidogenesis, which is done by mixing strongly acidifying and protein-stressed substrates or alkaline additives, or by cross-flow, but then only for substitution; second, according to the invention by means of monitored hydrolysis gas formation which is coupled to the intermediate formation (hydrolysis / acidogenesis), the latter being fed to post-fermentation after stagnating gas and acid formation with corresponding degradation of the biomass (A), the change containers then being strictly decoupled from the hydrolyzate storages; while they give off gas to the methanogenesis reactor (S) with a gas-tight lid, to which they are then coupled and from which they are also fed with digested sludge - at the end in the final phase, the change containers are replaced and thus the residual material without further refilling from the system directed to further processing. New containers of fresh biomass then replace those with the mined biomass. ( 1 thirdly, the feed of the intermediates from the reservoirs into the methane stages (S) FOS-TAC controlled by means of a concentrated liquid phase, which is obtained by solid-liquid phase separation or separation - this happens in each case so that the reactors with the lowest Fourth, the control of the processes (hydrolysis & acidogenesis, methanogenesis spatially separated and preferably no methanogenic populations in the buffer store incubated - which is achieved according to the invention by strict separation of the media and by the adjustment of the operating parameters with FOS / TAC value preferably with concentrated liquid phase exclusively enriched with hydrolytic and acidogenic populations, whereby always a sufficient part of this process water is transferred into the next cycle for inoculation, the other, however, continues to be used materially / energetically et (eg, digestion stages) and previously optimized with regard to the parameters (nutrients, pH, etc.). Method according to claims 1-6, characterized in that in a further alternating rhythm, coupled to the indicated sequences, ( 2 ), the replaceable containers are regularly filled with biomass (A) and depending on the substrate each after 1 to 12 days of fermentation with flooding / sprinkling (B, D) takes place an exchange of containers (A), which then decoupled from the process another 2-7 days contribute to the formation of methane after the addition of digested sludge, this changes in groups so that the discharge rhythm reciprocal to the working rhythm of the entire plant gem. Claim 2 functions suitably, and such that the fermentation phase (B) for the formation of an intermediate or acid is likewise coupled in accordance with the rhythm to the discharge phases of the hydrolyzate store (SP); In this case, therefore, there is always a part of the plant, ie a group fermentation container (AB) in the intermediate or acid formation process, the other half also alternately in the methane formation process, after mixing with digested sludge fractions in the final phase in decoupling of the hydrolyzate (SP). A method according to claim 1-7, characterized in that controller according to claim 3-4 carried out mainly on the basis of the parameters gas pressure, gas quantities and gas composition (H), and based on the nutrient and acid concentration, or the pH and the additive consumption, and Reaction of intermediates in the hydrolyzate to methane FOS / TAC regulated happens; Installation according to claim 1 to 4, characterized in that all processes are subject to a specific control and by means of a combination of at least two different starting materials (substrates / alkaline additives) the regulation of the pH is achieved between 5.0-6.0 and additionally by combination the substrates an optimized nutrient supply is done, thus bringing the total fermentation container and storage (A, B, SP) in the optimal working area and held there, under cyclic irrigation & flooding and discharge of laden with intermediates hydrolyzate or process water in the hydrolyzate (SP ) with concentration there, as well as monitoring the coupled to the decomposition hydrolysis gas / Additiverbrauch to stagnation for controlling the fermentation time of the cycles because the stagnation correlates with the optimum of acid or intermediate product formation, the subsequent implementation of the loaded hydrolyzate to methane mean els auomatized FOS-TAC analysis - hence FOS-TAC controlled happens. (in SP subgroups M, N, P, Q) A process according to claims 1-8, characterized in that the feed of the plant takes place by collecting feedstocks in the same exchange container (A) and transporting and fermenting them by introducing the exchange containers into reactor arrays (B) where they are connected to the fermentation ( V) and where the biomass is decomposed in the hydrolytic-acidogenic process stage, wherein the replaceable containers (A) are filled in exchange, here with gas-tight cover (B) are provided, which also contains a sprinkler system for process water, (D), and a Double bottom (J) for the discharge and first separation of the liquid phase, and all media lines and sensors, (H), which make the container part of the fermentation process, where the hydrolysis / acidogenesis takes place - and this after completed process again as a transport container for the transport of fresh biomass can be used if they are decoupled from the process again and beyond Process steps such as drying or composting can take place externally by changing the media connections (z. Hot air, oxygen, inoculum, etc). Plant as a modular system, ( 1 ) for the multi-stage fermentation of solid or liquid biogenic energy sources for the purpose of energy and raw material production, characterized in that the entire system system is designed mobile and modular as a container system (A, SP, K) with the fermenters designed as mobile garages (B) - that's it According to the invention, it is also possible, instead of the basic system described below, to use only the hydrolyzate stores as a fermentation system with the same destination in any number, depending on the feed substrates. The basic system is expandable and consists of the following components: 8 × interchangeable containers (transport or fermentation container) (A) 2 × memory modules with pH control (hydrolyzate storage) (SP) 1 × container module for methane production (K) 1 × control module for sensors and computer control (FOS / TAC) 4 × mobile garages as a heated fermentation room (B), inter alia, with quantitative gas measurement, gas-tight door, percolation cover, sieve tray inserts characterized in that the basic arrangement of the system acc. 1 Both modularly expandable, as well as existing systems (biogas / wastewater treatment plants) with existing methane level (S) are added, but also scaled for the first time ready modules for individual companies or municipalities are available and can be transported modularly. The plant is gem. the arrangement of 1 built up. Installation according to claim 10, that the fermentation step (A) of the process takes place in exchange containers in which the biomass remains through all the working phases of the plant, and from this energy, intermediates, compost and biogas is recovered from Biogasse in the form of methane gas or intermediates distributed directly or by transfer to connected bioreactors (eg sewage treatment plants) (S) to substitute them energetically and materially. Installation according to claim 1-11, that the technical implementation can be done depending on the application substrates in Rühkesselprinzip with exclusive use of the container store (SP) as bioreactors and with quasi-continuous or continuous feeding or in batches; wherein input concentrations up to 100 kg oTS / m ³ - preferably 30 kg oTS / m ³ - can be realized at fermentation times or hydraulic residence time of 1-12 days.

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