EP4046254A1

EP4046254A1 - Energy management method and system

Info

Publication number: EP4046254A1
Application number: EP20780618.3A
Authority: EP
Inventors: Michael Schelch; Wolfgang Staber
Original assignee: Individual
Current assignee: Individual
Priority date: 2019-10-15
Filing date: 2020-09-23
Publication date: 2022-08-24
Also published as: AT523088A1; WO2021073844A1

Abstract

The invention relates to an energy management method involving - at least one power grid, - at least one electrical energy-consuming process for producing at least one product and - at least one electrical energy-generating process, wherein the method is operated, on the basis of the control energy demand, in one of the following operating states: a) in the case of no control energy demand, in a normal mode in which the electrical energy-consuming process uses the energy from the electrical energy-generating process to produce at least one product, b) in the case of demand for negative control energy, in a storage mode in which additional electrical energy is fed from the power grid into the electrical energy-consuming process and thereby, in contrast to the normal mode, excess product is produced and stored, and c) in the case of demand for positive control energy, in an output mode in which the energy-consuming process is shut down or restricted and the electrical energy from the electrical energy-generating process is fed into the power grid.

Description

description

Process and system for energy management

The invention relates to a method and a system for energy management.

It is well known that the expansion of renewable energies is a declared goal of states and associations of states. As part of the 2030 Agenda for Sustainable Development, for example, the Austrian Federal Government has set itself the goal of reducing greenhouse gas emissions by 36% by 2030 compared to 2005. Furthermore, the share of renewable energies in gross final energy consumption is to be 45% to 50% by 2030. In addition, all electricity consumption in Austria should come from renewable energy sources in 2030.

The expansion of renewable energy naturally leads to higher fluctuations in the power grids. The fluctuating power feed brings increasing challenges. Among other things, the demands on the electricity markets, the electricity producers and the electricity grid operators are increasing.

The need for so-called control energy, which, as a reserve, balances out fluctuations in the electricity grid and thus prevents the grid from collapsing, increases considerably. Control energy intervenes, for example, when electricity consumption increases surprisingly, a conventional power plant fails or a sudden change in the weather significantly affects the forecast electricity production from renewable energy sources. Control energy compensates for fluctuations in the power grid within seconds ("primary reserve"), five minutes ("secondary reserve") or fifteen minutes ("minute reserve"). Control energy can not only be provided by electricity producers, but also by electricity consumers and electricity storage facilities (for a more precise definition of control energy, see below). Since electricity is often generated by means of renewable energies at a great distance from the electricity consumers, for example by means of offshore wind farms, the need for spatial compensation increases. The importance of systems and technologies for electricity storage is therefore increasing significantly; in particular, it can be assumed that there will be very high storage requirements in the future. Electricity storage systems are already considered to be a “key technology” for a successful energy transition.

There are currently four storage types available for storing electrical energy. These include mechanical storage (e.g. pumped storage power plants), electrochemical storage (e.g. batteries), electrical storage (e.g. capacitors) and chemical storage (e.g. hydrogen generated by electrolysis and converted in fuel cells or by means of a power-to-gas plant). As is well known, the storage of electrical energy is always associated with conversion losses. An economical operation of energy storage is therefore currently only possible to a limited extent. This is most likely to succeed when the energy storage system is also able to offer other system services (e.g. frequency maintenance through control and reserve power). In addition, the use of the memory mentioned as an example is associated with disadvantages known per se.

Pumped storage power plants have a number of far-reaching effects on the local and regional environment, both through construction and operation.

The local flora and fauna are significantly impaired by land use for the construction of storage basins and the necessary technical constructions (buildings, pipelines, network connection, etc.). This inevitably leads to undesired loss of biotope and further displacement processes. For geological reasons, only a limited number of pumped storage power plants can be built. The study EU ESTORAGE 2015 - "A new era of smart energy management" shows that pumped storage power plants with an expected capacity of 2.6 TWh can still be built in Western Europe. In batteries, due to their high energy density and the possible number of charging cycles, lithium-ion batteries are increasingly being used, which in addition to lithium can also contain other raw materials such as nickel, cobalt and manganese. Aluminum, graphite or silicon are used in other battery variants. In addition, copper is currently required for wiring the batteries. The degradation of the raw materials mentioned is known to be problematic. Lithium is extracted from salt lakes, for example. In South America it is customary to pump the brine (brine, the main component is water) out of the earth and evaporate the water. This process can lead to a lowering of the water table. Drought and the like can be the consequences. At the end of the battery life, it is also of crucial importance whether the batteries can be recycled or have to be disposed of. In any case, improper disposal of batteries harbors considerable environmental risks (e.g. fire hazard, groundwater contamination from leaking electrolytes). Lemer, the investment costs for batteries are currently relatively high compared to the service life, so that in the future these will only be economically viable energy storage devices if the production costs are reduced and the service life is extended.

In power-to-gas systems, electricity is used to generate hydrogen, which is converted into a gas with carbon dioxide with the help of a catalyst (methanation). This gas is usually not converted back into electricity directly, but used for other purposes. For example, the gas is fed into a gas network or used as fuel. At present, economical operation of power-to-gas systems is only possible with a very high system utilization.

In summary, it can be said that there are some ways of storing energy. These are often not economically viable and / or are associated with significant, negative effects on the environment.

One of the biggest problems here is that significant energy losses occur in all of the known energy storage devices. The amount of energy that can be "extracted" from the energy storage device is always smaller than the amount of energy that is "put into it". In terms of their energy balance, they are therefore not the same amount. The invention is therefore based on the object of providing an energy management concept that is significantly more favorable and advantageous with regard to its energy balance.

The object set is achieved according to the invention by a method for energy management with the participation of

- at least one power grid,

- At least one electrical energy consuming process for the production of at least one product and

- at least one electrical energy generating process,

- the method being operated in one of the following operating states as a function of the control energy requirement: a) when there is no control energy requirement in normal operation, in which the electrical energy consuming process uses the energy of the electrical energy generating process to produce at least one product, b) if required negative control energy in a storage operation, in which additional electrical energy is fed into the electrical energy-consuming processes from the power grid and an excess of product is produced in comparison to normal operation and this is stored and c) if positive control energy is required in a delivery operation in which the energy-consuming process is shut down or throttled and the electrical energy of the electrical energy-generating process is fed into the power grid.

Furthermore, the object set is achieved according to the invention by a system for energy management which comprises the following:

- at least one power grid,

- at least one first system component for generating electrical energy,

- At least one second system component for manufacturing at least one product using electrical energy from the first system component,

- At least one warehouse for storing excess product and - An electronic control, which feeds electrical energy into the second system component in the event of negative control energy from the power grid and, in the case of positive control energy, throttles or switches off the supply of electrical energy from the first system component to the second system component and at least for the electrical energy generated in the first system component Part feeds into the power grid.

The method according to the invention and the system according to the invention thus completely dispense with energy storage devices in the conventional sense. Namely, at least one electrical energy-consuming process for the production of at least one product (or the corresponding system component), at least one electrical energy-generating process (or the corresponding system component) and a power grid are combined in a special way depending on the control energy requirement. decoupled. In the process, negative control energy is used to increase the productivity (performance) of a process that produces one or more products (product (s) surplus). Such a process is characterized in particular by the fact that it is easy to automate, can be switched on and off quickly and is not time-critical in its implementation, and can therefore be carried out at any point in time. The storage of electrical energy is completely dispensed with, products are stored. If positive control energy is required, the electrical energy of the electrical energy generating process is fed into the power grid. The system according to the invention absorbs energy and makes energy available so that it behaves like an energy store to the outside, without being or having one. As a result, the system and the method work - in contrast to currently known energy storage systems - at least essentially the same amount (none

Conversion losses). Provided that no energy is required for the storage of the products, for example by cooling or stirring, the process even works with the same amount. Furthermore, a higher “pseudo energy storage density” can be achieved than with conventional energy storage systems (for a more detailed explanation see point 4). The extent to which the “pseudo-energy storage”, that is to say the product storage, can take place is only dependent on the size of the store or stores which accommodates the at least one product obtained in step b), ie stores. The products are generally suitable for long-term storage, so that seasonal fluctuations in demand for electrical energy can also be ideally balanced out. For example, the stronger solar radiation that prevails in the summer months can be used to create a product (s) surplus. In the winter months, which are less profitable in terms of solar radiation, energy is then made available. The process that consumes at least one electrical energy for producing at least one product can advantageously be operated economically in normal operation. With conventional storage power plants, such as a pumped storage power plant, there is no “normal operation” in this sense.

In the following, preferred embodiments of the method are first discussed and then preferred embodiments of the system are discussed in greater detail.

According to a preferred embodiment of the method, the product or products which is or are produced with the process that consumes electrical energy is liquid or gaseous. Liquid and gaseous products are easy to handle logistically, so that the relevant process steps can be carried out in a reliable and simple automated manner. In particular, compared to solid products, the products can be stored in a space-saving manner and easily transported or forwarded using pumps, pipes, valves and the like.

It is preferred if the process that consumes electrical energy is or are used to produce a product or products which can be stored in a stable manner without additional energy expenditure, such as cooling, for example. In this case, the method advantageously works with the same amount.

According to a further preferred embodiment of the method, the process consuming electrical energy is an electrolysis process, in particular an electrochemical membrane process, metal extraction electrolysis, electrochemical cleaning of metals, a process falling under the term electroplating, organic electrosynthesis or water electrolysis. Electrolysis processes are very energy-intensive, they therefore enable extremely high pseudo-energy storage densities (see point 4.2.2, final result 3). They are also characterized by their short start-up times, so that storage operation can be started particularly quickly if negative control energy is required. In addition, electrolysis processes can be shut down or throttled quickly.

In a further preferred embodiment, the process consuming electrical energy is an evaporation, in particular an evaporation of water from starting materials containing water. Evaporation of water is also an energy-intensive process. The concentrate that remains after evaporation therefore has a high pseudo energy storage density (see point 4.2.1, final result 2) and is generally stable in storage. It can therefore be stored at ambient temperature without the use of additional energy, so that the method works in the same amount and the storage costs are low. The evaporation can be quickly shut down or throttled when there is a need for positive control energy and quickly started when there is a need for negative control energy.

In particular with regard to process logistics, it is advantageous if at least one product is produced by means of the process that consumes electrical energy, which product is at least partially used as a starting material for the process that produces electrical energy.

In a further preferred embodiment, at least one water-containing, biological starting material, in particular a biogenic raw material or a biogenic residue, is used for the process that consumes electrical energy. Such starting materials are often inexpensive to procure and store and are usually available in large quantities.

It is particularly preferred if organic waste or wastewater is used as the biogenic residue, furthermore the biogenic fraction arising from mechanical-biological waste treatment, agricultural and forestry by-products, biogenic production residues, liquid manure, fermentation residues from a biogas plant, sewage sludge, slaughterhouse waste, animal meal, residual forest wood , Leftovers out the forest and wood industry production, landscape maintenance material, waste from gardens, parks and cemeteries, biowaste, excrement from animal husbandry and / or greenery along the road is or are used. The biogenic residues mentioned are available inexpensively, with some, for example sewage sludge, sometimes even having a negative purchase price. These residues can also be easily stored, for example in stacking basins.

In a further preferred embodiment of the method, several processes consuming electrical energy, in particular at least one evaporation and at least one electrolysis process, preferably an electrochemical membrane process, are involved. A virtual power plant can be created by using a large number of such processes.

The electricity network involved in the process is preferably an interconnected network.

It is also preferred if the process consuming electrical energy runs continuously in normal operation. Such a process quickly adapts to the respective balancing energy requirement.

In a particularly favorable variant of the method, the processes that consume electrical energy include the following successive steps: i. Mixing a biological starting material containing organic compounds and water with an alkaline hydrolysis agent dissolved in water to form a hydrolyzed medium, ii. Heating and evaporation of the hydrolyzed medium to form a vapor and a concentrate, iii. a) in normal operation: use of the concentrate to generate electrical energy by means of the electrical energy generating process, b) in storage mode: use of a portion of the concentrate to generate electrical energy by means of the electrical energy generating process as well as storage of the further concentrate, c) in the dispensing operation: Use of the concentrate stored in the storage operation to generate electrical energy by means of the electrical energy-generating process.

In this variant, it is advantageous if the step i. hydrolysis agent used is at least one from the group consisting of sodium hydroxide, sodium carbonate, sodium hydrogen carbonate, lithium hydroxide, lithium carbonate, lithium hydrogen carbonate, potassium hydroxide, potassium carbonate, potassium phosphate, potassium hydrogen phosphate, potassium dihydrogen phosphate or dipotassium hydrogen phosphate. These hydrolysis agents can advantageously be recovered by means of electrolysis processes.

It is also advantageous in this variant if the in step ii. accumulating vapors are condensed and converted into an ammonia solution with the addition of at least one acidic process auxiliary in at least one electrolysis cell. The ammonia solution is a particularly valuable chemical compound.

In addition, it is advantageous in this variant if in step iii. the concentrate to generate electrical energy is heated in a reactor to up to 700 ° C and the resulting gases are converted in a combined heat and power plant.

In addition, it is advantageous in this variant if the in step iii. The residue remaining in the reactor is mixed with water to form an eluate, with at least part of the eluate in an electrolysis cell being used for step i. suitable hydrolysis agent is formed.

In a further particularly favorable variant of the method, the processes that consume electrical energy include the following successive steps:

I. Evaporation of a biological starting material containing organic compounds and water to form a vapor and a concentrate,

II. A) in normal operation: converting the concentrate in a biogas plant, whereby a digestate is formed and this is discharged from the biogas plant, b) in storage mode: feeding in electrical energy in step I, so that an excess of concentrate is formed, which is subsequently stored in the biogas plant, c) in delivery mode: formation of biogas from the concentrate stored in storage mode and generation of electrical energy from the biogas .

The advantages of this variant are detailed under point 2 (see below). A particular advantage is that the biogas plant is used as an "internal storage" at the same time. There is therefore no need for an “external product store”.

Further preferred embodiments relate to the system according to the invention.

The system preferably comprises a multiplicity of first system components and / or a multiplicity of second system components. Accordingly, large amounts of electrical energy can be taken from the power grid or fed into it.

It is also advantageous if a first system component is a block-type thermal power station. A combined heat and power plant is preferably operated at the place of heat consumption, it can also feed useful heat into a local heating network and advantageously uses the principle of combined heat and power.

In addition, it is preferred if one or more second system component (s) is or are provided, which is or are an evaporator, an electrolysis cell and / or a biogas plant. The advantages of these system components have already been pointed out in connection with the preferred embodiments of the method.

Further features, advantages and details of the invention will now be explained in more detail with reference to the drawing. Show it

Fig. 1 schematically and exemplarily control energy flows within an Austrian federal state, 2 shows a block flow diagram of a system S1 for energy management in normal operation according to a first exemplary embodiment,

2a and 2b are diagrams for further explanation of the system S1,

Fig. 3 is a block flow diagram of the system S1 in storage mode,

4 shows a block flow diagram of the system S1 in the delivery mode,

5 shows a block flow diagram of a system S2 for energy management in normal operation according to a second exemplary embodiment,

6 shows a block flow diagram of the system S2 in storage mode and

7 shows a block flow diagram of the system S2 in the delivery mode.

The invention relates to a system and a method for energy management. The system comprises at least one system component for generating electrical energy, at least one system component for producing at least one product using electrical energy, at least one power grid, in particular an interconnected grid (electrically connected power grids), and an electronic control that operates or implements the method. At least one electrical energy-generating process, at least one electrical energy-consuming, at least one product-generating process, and a power grid, in particular an interconnected grid, are involved in the method.

First of all, definitions used in the description that are known per se are briefly reproduced.

Control energy (control power, reserve power): Control energy refers to the energy that a power grid operator needs to compensate for unforeseen fluctuations in power in the power grid (fluctuations in the power frequency). Deviations between power generation and power consumption are therefore compensated for by using control energy so that the stability of the power grid is not endangered. When using control energy, electrical energy is therefore taken from the power grid or fed into it. Control energy can be provided by electricity producers, electricity consumers and electricity storage systems, for example.

Negative balancing energy

If the electrical energy fed into the power grid exceeds the electrical energy taken from the power grid at the same time, i.e. the supply of electrical energy is greater than the demand, there is a power surplus in the power grid. The electricity network operator “needs negative control energy” from electricity consumers, who withdraw electrical energy from the electricity network over a certain period of time.

Positive balancing energy

To compensate for increased demand for electrical energy when there is insufficient supply of electrical energy, the power grid operator needs positive control energy. It is necessary to feed additional electrical energy into the power grid over a certain period of time.

The explanations given below with reference to FIG. 1 are to be understood as purely exemplary. Fig. 1 shows a view of the Austrian state of Styria. A power grid operator and a number of power consumers and / or power generators are indicated. A large number of lines symbolize a power grid, through which negative and positive control energy flows to compensate for fluctuations in the power frequency. The flow of negative balancing energy is through a the flow of positive balancing energy is indicated by a "+". For example, the electrical energy generated by a biogas plant can be fed into the power grid to compensate for increased demand (positive control energy). As an example, the power grid operator supplies a temporary one that is above current demand Excess electricity (negative control energy) to a power-to-gas system and to an industrial wastewater treatment facility.

In Fig. 1, five systems S1 to S5 are indicated by way of example. Lines marked with “±” and running between the power grid operator and systems S1 to S5 symbolize the possibility of supplying each of the systems S1 to S5 with a temporary surplus of electricity in the power grid (negative control energy) as well as the option of using each of these systems S1 to S5 insufficient supply of electrical energy to make it available for feeding into the power grid (positive control energy).

In the exemplary embodiments, valuable chemical compounds are obtained from organic and inorganic compounds contained in waste by means of the energy-consuming processes. A valuable chemical compound is understood to be one that is used, for example, in industry and is therefore suitable for sale. Parts of the systems S1 to S5 can in particular correspond to the device disclosed in the patent application AT 520454 A2 in a correspondingly adapted manner. Another suitable system is the device from the as yet unpublished Austrian patent application with the official file number A50630 / 2018. The electrolysis cells used in this case are designed in particular as described in AT 520454 A2 or A50630 / 2018.

In the following, first the system S1, including the associated method, and then the system S2, also including the associated method, are explained with reference to FIGS. 2 to 7. Material flows are indicated by solid lines, the flow of electrical energy is indicated by dashed lines. The quantities given for the substance flows in FIGS. 2 to 4 are to be understood as purely exemplary.

1. Description of the system S1 (Fig. 2 to Fig. 4, including Fig. 2a and Fig. 2b)

A possible waste for the energy-consuming process of system S 1 is liquid manure, for example. Liquid manure consists largely of water and inorganic and organic compounds dissolved or suspended in the water. To the ones in the water The inorganic compounds contained include, in particular, potassium salts, amines, ammonium, amides, such as urea, nitrates, nitrites and phosphates. The organic compounds contained in water include, in particular, fats, proteins, carbohydrates and lignins. As will be explained in more detail, valuable chemical compounds can be obtained from these organic and inorganic compounds. Furthermore, electrical energy can also be obtained from the organic and inorganic compounds to produce the valuable chemical compounds, as will also be described below.

Table 1 shows examples of the compounds commonly referred to as nutrients found in manure.

Table 1: Composition of manure

Typical liquid manure has a dry matter content (= component of a substance that remains after subtracting the mass of the water it contains) of around 3% to 10%.

1.1 System S1 - normal operation

As FIG. 2 shows, during normal operation of the system S1, liquid manure is fed from a liquid manure store 1 to a mixer 2. A potassium hydroxide solution (aqueous potassium hydroxide solution, "KOH") from a potassium hydroxide store 3 and, preferably, an eluate containing potassium (hydrogen) carbonate (s) and potassium phosphate (s) from an eluate store 10 are also fed into the mixer 2, wherein the eluate and the potassium hydroxide solution are preferably mixed before entering the mixer 2. The formation (origin) of the potassium hydroxide solution and the eluate will be explained in more detail later. The supplied potassium hydroxide solution or the supplied mixture of potassium hydroxide solution and eluate has a pH of preferably at least 12.0. The liquid manure is mixed with the supplied potassium hydroxide solution or the supplied mixture in the mixer 2, whereby a liquid and at least largely homogeneous medium is formed.

The medium formed is passed on from the mixer 2 into an evaporator 4, which is based in particular on the principle of an evaporator with a heating jacket and mechanical vapor compressor. In the evaporator 4, the medium is heated to 70 ° C. to 140 ° C., as a result of which all organic compounds present in the medium are alkaline hydrolyzed, that is to say the molecules of the organic compounds are broken down (split). As a result of the use of potassium hydroxide solution, organic potassium salts form at least from the majority of the organic compounds from the liquid manure (known to have at least one anion of an organic acid, ie a carboxylate group R-COO-) and from the phosphates present, potassium phosphate (e ), the organic potassium salts and the potassium phosphate (s) going into solution, i.e. dissolving in the medium.

During the hydrolysis, a vapor forms in the evaporator 4. This consists of water vapor and gaseous nitrogen compounds (ammonia, amines) and is passed from the evaporator 4 into a condensate store 5, in which it condenses and can be temporarily stored if required. The condensate formed from the vapor is fed with phosphoric acid (H3PO4) into at least one electrolysis cell 6, in which phosphoric acid (H3PO4) was generated and is continuously generated. The nitrogen compounds contained in the condensate form ammonium phosphates, which at least for the most part ^{dissociate to form ammonium (NH4 +} ) and phosphate ions. The addition of phosphoric acid also acidifies the condensate, which shifts the dissociation equilibrium between ammonia and ammonium (NH3 + H3q ⁺ NH4 ⁺ + H2O) in the direction of ammonium (NH4 ⁺ ) in the condensate. In contrast to ammonia, ammonium is accessible to an electrochemical reaction. In the electrolysis cell 6, the phosphoric acid (H3PO4), an aqueous ammonia solution (NH3 - H2O) and hydrogen are then obtained. The ammonia solution, the hydrogen and any excess Phosphoric acid are derived from the electrolytic cell 6, they belong to the valuable chemical compounds.

The liquid “hydrolyzed” medium formed in the evaporator 4 and remaining in it contains the organic potassium salts and potassium phosphate (s) already mentioned and dissolved in it. The hydrolyzed medium is derived from the evaporator 4 and, as will be explained, further processed. First, however, the effect of hydrolysis on the pumpability of the medium is explained with reference to FIG. 2a.

2a shows an exemplary diagram, not to scale, in which the content of organic dry matter in% (oTS content) is plotted on the abscissa and the viscosity is plotted on the ordinate without any dimensions or scaling. The viscosity increases according to the arrow pointing upwards. The organic dry matter (OTS), also called dry matter, is known to be the proportion of organic components (organic compounds) of a substance (here the medium) after complete removal of water and complete removal of all mineral components. The dashed line shows the viscosity for the original liquid manure from the liquid manure store 1 as a function of its ODM content (in Fig. 2a: “Liquid manure untreated”). The solid line shows the viscosity of the hydrolyzed medium as a function of its ODM content (in Fig. 2a: "Liquid manure hydrolyzed"). Furthermore, a horizontal line denoted by shows the viscosity up to which the Liquid manure or the medium can be pumped using conventional means. If the viscosity of the liquid manure or the hydrolyzed medium exceeds that indicated by the line Viscosity value, the liquid manure or the hydrolyzed medium can essentially no longer be pumped. The temperature of the liquid manure or the hydrolyzed medium is an example of 100 ° C (in Fig. 2a: T = 100 ° C). It can be seen that the original, untreated liquid manure is already so viscous that it can no longer be pumped from an ODM content in the range between 15% and 20%. In contrast to this, the hydrolyzed medium from the evaporator 4 can be pumped up to an oTS content of almost 80%.

The hydrolysis process therefore enables a pumpable medium with a - compared to the starting product (the original liquid manure) - significantly higher ODM content receive. Due to its significantly higher oTS content, the hydrolyzed medium is therefore referred to below as “concentrate”.

According to FIG. 2, the concentrate formed in the evaporator 4 is passed on to a reactor 7 in which the concentrate is heated to up to 700 ° C., in particular up to 400 ° C., as a result of which the organic compounds contained in the concentrate are thermally decomposed and gases are formed. The gases are fed into a block-type thermal power station 8, in which electrical energy and heat are generated from the gases in a known manner. The aforementioned evaporator 4, the at least one electrolytic cell 6 and at least one electrolytic cell 9 are operated with this electrical energy.

FIG. 2b shows a further exemplary diagram which illustrates further advantages of the previously carried out hydrolysis. The temperature in the reactor 7 in ° C. is plotted on the abscissa and the amount of organic dry matter which is relatively degraded during heating in the reactor 7 is plotted on the ordinate. The solid line shows the relatively broken down amount of organic dry matter for the concentrate introduced into the reactor 7 ("liquid manure treated" in FIG. 2b) as a function of the temperature in the reactor 7. The dashed line shows the relatively broken down amount of organic dry matter for Original, untreated liquid manure introduced into the reactor 7 (“untreated liquid manure” in FIG. 2b), which, however, is not provided for in the present process and is only used for comparison and explanation. It can be seen that in the temperature range from 200 ° C. to 400 ° C. the amount of organic dry matter relatively degraded in reactor 7 is significantly higher when using the concentrate than when using untreated liquid manure. If untreated liquid manure is heated to 400 ° C., for example, in the reactor 7, only 40% of the organic dry matter content of the liquid manure has been decomposed. When using the concentrate (= hydrolyzed and evaporated liquid manure), the organic dry matter contained in it is at least substantially completely decomposed at a temperature of 400 ° C (continuous line in Fig. 2b at 400 ° C / 100% relatively degraded oTS amount) . As FIG. 2b shows, the use of the concentrate is significantly more favorable in terms of energy - compared to untreated liquid manure - since - compared to untreated liquid manure - significantly larger percentages of the amounts contained in each case are present even at lower temperatures organic compounds are broken down. In the reactor 7, therefore, larger percentages of gas are obtained from the concentrate - compared to the untreated liquid manure.

A solid, in particular powdery residue of inorganic compounds remains in reactor 7, which includes poorly soluble or insoluble inorganic compounds ("ash") and, due to the use of potassium hydroxide, water-soluble inorganic potassium salts (known to have an anion of an inorganic acid) . The ash mainly includes oxides and (bi) carbonates of various metals. In the exemplary embodiment, the water-soluble inorganic potassium salts include potassium (hydrogen) carbonate (s) and potassium phosphate (s). The solid residue is discharged from the reactor 7 and mixed with water, whereby an eluate is formed. As is known, an eluate is understood to be a mixture of a solvent and substances dissolved in it. The solvent of the eluate in question is therefore water, in which the water-soluble inorganic potassium salts dissolve, so that the eluate is an electrolyte solution. The eluate is passed into an eluate store 10, the ash preferably being separated off, for example filtered off, in a manner not shown before it reaches the eluate store 10.

As has already been mentioned in the explanations of the normal operation of the system S 1, part of the eluate is preferably passed from the eluate store 10 into the mixer 2, the ash that may not yet be separated being separated off. Furthermore, eluate is passed from the eluate store 10 into the already mentioned electrolysis cell 9, the ash that may not yet be separated being also separated off.

An eluate freed from ash thus reaches the electrolysis cell 9, in which potassium hydroxide in the form of potassium hydroxide (KOH) and phosphoric acid (H3PO4) are formed from the eluate. The potassium hydroxide (KOH) and the phosphoric acid (H3PO4) are derived from the electrolysis cell 9, they represent further valuable chemical compounds is not required for the hydrolysis of the manure, can be removed. During normal operation of the process, the processes that consume electrical energy and produce products run in a continuous manner, i.e. continuously over time. The fill levels in the potassium hydroxide store 3, in the condensate store 5 and in the eluate store 10 fluctuate to a certain extent, but are essentially constant. As an example, normal operation is carried out with a slurry input of 30 kg OTS / h (mass of organic dry matter per hour) and a potassium hydroxide input of 6 kg / h. At these throughputs, the evaporator 4 and the electrolysis cell 9 do not run at maximum power but, for example, at 50% of the maximum power. As is known, the output is understood to mean the amount of a product (here, for example, the concentrate) generated in a unit of time.

In the case of system S 1, the system component for generating electrical energy is the combined heat and power unit 8. The process that generates electrical energy therefore takes place in the combined heat and power unit 8. There are four system components for the production of products, namely the evaporator 4 (produces the concentrate and the condensate during normal operation of the process), the reactor 7 (produces the eluate and gases during normal operation of the process), and the electrolytic cell 6 (produces during normal operation of the process Ammonia solution and phosphoric acid) and the electrolysis cell 9 (generated during normal operation of the process potassium hydroxide and phosphoric acid). Ammonia solution, phosphoric acid and potassium hydroxide are the end products. Furthermore, potassium hydroxide is a basic process aid that can be stored for the hydrolysis of liquid manure. The phosphoric acid generated in the electrolysis cell 6 also represents an acidic processing aid. The concentrate, the condensate and the eluate are intermediate products that can be stored.

1.2 System S1 - storage operation

According to FIG. 3, excess electrical energy present in the power grid during storage operation (the power grid operator needs negative control energy) is fed into the system S 1 by the power grid operator.

This electrical energy is fed to the evaporator 4 and the electrolysis cell 9. Compared to normal operation, the liquid manure use is reduced to 60 kg OTS / h and that in the Mixer 2 conducted amount of potassium hydroxide solution doubled to 12 kg / h. The amount of potassium hydroxide solution formed in the electrolytic cell 9 increases to 20 kg / h. The amount of phosphoric acid formed per hour in the electrolysis cell 9 also increases.

Compared to normal operation, twice the amount of liquid medium is now put through in the evaporator 4. Of the concentrate formed in the evaporator 4, 30 kg OTS / h are passed into the reactor 7 and the further 30 kg OTS / h are passed into a concentrate store 11. More eluate is withdrawn from the eluate store 10 than is introduced into it (originates from the residues remaining in the reactor 7, mixed with water), the withdrawn eluate being passed to the electrolysis cell 9 and, if necessary, to the mixer 2. Excess potassium hydroxide can be derived from the potassium hydroxide store 3. If necessary, the eluate also flows exclusively into the electrolysis cell 9 during storage operation.

As soon as the power grid operator no longer needs negative balancing energy, the system returns to normal operation (Fig. 2).

In the case of system S1, two of the four system components for manufacturing products (the evaporator 4 and the electrolysis cell 9) are thus supplied with additional energy (negative control energy) during storage operation.

1.3 System S1 - dispensing operation

4 shows the system S1 in the dispensing mode. The power grid operator needs positive balancing energy.

The mixer 2, the evaporator 4 and the electrolysis cells 6 and 9 are temporarily not operated. The electrical energy obtained in the block-type thermal power station 8 is fed to the electricity network operator. In the exemplary embodiment, to generate energy from the concentrate store 11, the concentrate collected in this during storage operation is passed into the reactor 7, in which gases are generated from the concentrate, from which electrical energy is obtained in the block-type thermal power station 8. The electric Energy is fed to the power grid operator. The residue remaining in the reactor 7 is mixed with water and passed on to the eluate store 10.

In the case of system S 1, in the described embodiment, all system components for the production of end products are shut down in the dispensing operation (electrolysis cells 6 and 9). The system component for generating electrical energy (block-type thermal power station 8) supplies the generated electrical energy to the power grid. Alternatively, the supply of electrical energy to the system components for the manufacture of products can be throttled.

2. Description of the system S2 (Fig. 5 to Fig. 7)

2.1 System S2 - normal operation

5 shows the system S2 in normal operation. As indicated laterally by a bracket labeled “analog system S1”, the system S2 represents an extension or a special embodiment of the system S1, the system S2 with a second evaporator 4 ', a second condensate store 5', a second Electrolysis cell 6 ', a second combined heat and power unit 8' and a biogas plant 12 is expanded. In comparison to the system S1, as also shown in the exemplary embodiment, the concentrate store 11 can advantageously be dispensed with.

Liquid manure is introduced from the liquid manure store 1 into the evaporator 4 ', in which the liquid manure is heated and water is evaporated from this. The liquid manure is "evaporated" in such a way that the liquid manure concentrate remaining in the evaporator 4 'has a dry matter content of preferably 15% to 25%. The vapor that forms when the liquid manure is evaporated contains primarily ammonia and is passed into the condensate store 5 'and condenses in it. In the electrolysis cell 6 ', phosphoric acid (H ₃ PO ₄ ), an aqueous ammonia solution (NH ₃ - H ₂ O) and hydrogen are obtained from the condensate.

The liquid manure concentrate remaining in the evaporator 4 'is suitable - in contrast to the original liquid manure - due to its lower water content and its lower content of nitrogen compounds - as a starting material for the biogas plant 12 Biogas plant 12 occurring nitrogen inhibition of the bacteria advantageously avoided. In addition, with the liquid manure concentrate - compared to the original liquid manure - a higher "digestion chamber load"("volumeload") can be achieved. The digester load indicates, as is well known, the maximum amount of organic dry matter that can be added to the biogas plant without the underlying biological process "overturning".

In the biogas plant 12, the liquid manure concentrate is converted into biogas, which is fed into the block-type thermal power station 8 ‘. The combined heat and power unit 8 ‘provides the electrical energy for the evaporator 4‘.

The digestate remaining in the biogas plant 12 (= remaining liquid and / or solid residue) again contains, among other things, ammonia and / or ammonium, which was formed by the breakdown of proteins. The further processing of the digestate takes place in the same way as the processing of liquid manure already described in System S1. In the next step, the digestate is passed on to a mixer 2, where it is mixed with a potassium hydroxide solution and optionally with eluate.

One advantage of using a biogas plant is that a valuable chemical compound, namely the aqueous ammonia solution (NEE - EbO) discharged from the cell 6, is obtained from part of the ammonia contained in the liquid manure without the use of potassium hydroxide. Depending on the application, this can be advantageous with regard to the energy balance. The amount of potassium hydroxide required for further processing of the fermentation residue is less - compared to direct use of the liquid manure, as provided for in system S1 (FIGS. 2 to 4). The S2 system is particularly beneficial when continuously large amounts of liquid manure accumulate.

2.2 System S2 - storage operation

6 shows the system S2 in storage mode. Excess electrical energy supplied by the power grid operator (negative control energy) is fed to the evaporator 4 'connected upstream of the biogas plant 12, so that more liquid manure concentrate, i.e. an excess of liquid manure concentrate, is formed compared to normal operation. The Liquid manure concentrate continues to slide into the biogas plant 12, which is operated as in normal operation (see point 2.1), so that an excess of liquid manure concentrate remains in the biogas plant 12 and is stored in this way in the biogas plant 12. The biogas plant 12 therefore takes on the storage function and thus serves temporarily as a store for the liquid manure concentrate.

2.3 System S2 - delivery operation

7 shows the system S2 in the delivery mode. The evaporator 4 ‘connected upstream of the biogas plant 12 is shut down. The liquid manure concentrate stored in the biogas plant 12 is converted into gases, from which electrical energy is generated in the combined heat and power unit 8, which is fed into the power grid. The digestate is converted as in normal operation (see point 2.1) and in storage mode (see point 2.2).

3. Other variants

3.1 Variants of the exemplary embodiments shown and described in the figures

3.1.1 Biological starting materials for the process that uses electrical energy and produces at least one product

The biological starting material is in particular a water-containing biogenic raw material or a biogenic residue (biogenic waste). Biogenic residues are, in particular, organic waste / wastewater, the biogenic fraction that occurs during mechanical-biological waste treatment, agricultural and forestry by-products, biogenic production residues, the already mentioned liquid manure, the already mentioned digestate, sewage sludge, slaughterhouse waste, animal meal, residual forest wood, residues the forest and wood industry production and landscape maintenance material, waste from gardens, parks and cemeteries, organic waste, excrement from animal husbandry, greenery along the road, etc.

3.1.2 Variants of the reactor 7

According to a first preferred variant, the reactor 7 is a fixed bed reactor. The concentrate introduced is applied to a fixed bed (solid bed or packing) located in the reactor. Subsequently, the fixed bed is heated by a hot gas flows through. The concentrate forms gases which, as already described, are routed to a block-type thermal power station, for example. The solid, in particular powdery, phase remaining in the fixed bed reactor is discharged, for example, via a rotating grate or the like.

According to a second preferred variant, the reactor 7 is a stirred tank which is operated either continuously or discontinuously and in which there is a heat transfer medium, which can be in the form of a powder, for example, or is a heat transfer oil, in particular a thermal oil. The concentrate introduced into the stirred tank is heated to, in particular, approximately 350 ° C. under atmospheric pressure and / or to preferably approximately 400 ° C. under slight excess pressures (approx. 1 bar). The solid, in particular powdery phase remaining in the stirred tank, originating from the originally introduced concentrate, is separated from the heat transfer medium by elution, sedimentation, filtration or the like and the heat transfer medium is returned to the stirred tank. The heat transfer medium can either be heated in the stirred tank or outside the stirred tank.

3.1.2 Basic processing aids

In the exemplary embodiment described, the potassium hydroxide solution forms a basic processing aid, by means of which the inorganic and organic compounds contained in the starting material are made available for material utilization (hydrolysis of the organic compounds). In particular, sodium hydroxide, sodium carbonate, sodium hydrogen carbonate, lithium hydroxide, lithium carbonate, lithium hydrogen carbonate, potassium hydroxide, potassium carbonate, potassium phosphate, potassium hydrogen phosphate, potassium dihydrogen phosphate, dipotassium hydrogen phosphate or a mixture of these substances come into consideration as process auxiliaries.

3.1.3 Acid process auxiliaries

The phosphoric acid, which is used to acidify the condensate, also forms a process aid. Instead of phosphoric acid, another suitable inorganic acid, in particular sulfuric acid, can be used. This will, as for the phosphoric acid described, generated in the electrolytic cell 6. Instead of phosphates, corresponding sulfates are formed when sulfuric acid is used. As already explained, ammonium (NH4 ⁺ ) or dissolving ammonium salts are formed, which are accessible to an electrochemical reaction.

3.1.4 Use of a scrubbing column for gas scrubbing

The vapor formed in the evaporator 4, 4 ‘and containing nitrogen compounds can be passed from the evaporator 4, 4 in directly into a scrubbing column, where one of the acids mentioned can be added. A corresponding condensate forms, as explained under point 1.1 and point 3.1.3. The condensate is, as described, passed into the condensate store 5, 5 'or it is in particular passed into a receiving water from which it flows on into the electrolytic cell 6, 6'.

3.1.5 Use of an ion exchanger

The vapor formed in the evaporator 4 and containing nitrogen compounds can also be passed over an ion exchanger which is regenerated with one of the acids mentioned, the acid coming from the electrolysis cell 6, 6 ‘. Corresponding sulfates or phosphates are formed in the ion exchanger. Depending on the configuration, the condensate storage 5, 5 ‘can be dispensed with.

3.2 Examples of possible processes that use electrical energy and produce at least one product

The process that consumes electrical energy produces, in particular, at least one storable product. Energy-intensive processes that require large amounts of electrical energy and - in relation to the volume of product produced - produce as little product as possible are particularly favorable, because high “pseudo energy storage densities” can be achieved with such processes (see point 4).

Particularly suitable processes are electrolysis processes, in particular electrochemical membrane processes, metal extraction electrolysis, the electrochemical cleaning of metals, the processes falling under the term “electroplating” (for example electrochemical metal deposition or electrochemical metalworking), organic electro-synthesis and water electrolysis.

The "products" resulting from these processes that consume electrical energy form "pseudo-energy stores". The expression pseudo-energy storage is intended to make it clear that no electrical energy is stored per se, but the energy is "objectified" or available as an equivalent after the work has been carried out in the respective product formed (see also point 4). In the first exemplary embodiment (system S1) in question, the concentrate emerging from the evaporator 4 and the potassium hydroxide solution produced in the electrolysis cell 9 and the phosphoric acid produced in this form pseudo-energy stores.

4. Calculations for the "pseudo energy storage density"

The following exemplary and approximate calculations are for illustration purposes only. The method according to the invention is compared with a conventional pumped storage power plant with regard to its “pseudo energy storage density”.

4.1 Pumped storage power plant

The potential energy of a pumped storage power plant can be calculated using the following equation: potential energy m [kg] mass of the pumped water g [m / s ² ] acceleration due to gravity, g ~ 9.81 m / s ² h [m] height above the ground (height difference between the deep basin and the storage basin)

The following assumptions are made for the calculation:

The height difference h is 100 m. - The overall efficiency of the pumped storage power plant is 80% or 0.8.

From equation 1 it follows:

In order to arrive at the “real” pseudo energy storage density, the overall efficiency of the pumped storage power plant and the storage requirements of the “educt” (water in the deep basin) and the “product” (water in the storage basin) are taken into account. The storage requirement is 2m ³ , as the water first takes up 1m ³ in the deep basin and then 1m ³ in the storage basin. The following therefore applies:

Using the pumped storage power plant, 0.11 kWh per cubic meter of water can be “pseudo-stored” in the example. This amount of electrical energy equivalent is present in every cubic meter of water pumped up, which thus forms the pseudo energy store.

4.2 Method According to the Invention - System S1

In the case of system S1, the excess energy (negative control energy) is fed to the evaporator 4 and the electrolysis cell 9. As already mentioned, the concentrate formed in the evaporator 4 and the potassium hydroxide solution generated in the electrolysis cell 9 and the phosphoric acid generated in this form the pseudo-energy storage device (see 3.2). Calculations for the pseudo energy storage density of the concentrate and the phosphoric acid are then carried out. In the calculations for the pumped storage power plant, the aspect of the water storage requirement was already taken into account in equation 1 through the water density. In the calculations for the method in question, the aspect of storage requirements is only taken into account at the end.

4.2.1 On the pseudo-energy storage concentrate Calculations are carried out ^{for 1m 3 manure.} The pseudo energy storage density of the concentrate can be calculated from the electrical energy (work) which the evaporator 4 needs to form the concentrate.

The following assumptions are made for the calculation:

- The manure has a dry matter content of 5%. It therefore consists of 95% water and 5% dry matter.

- The liquid manure is evaporated in an evaporator with a mechanical vapor compressor, whereby the condensation of the steam takes place at a temperature of 90 ° C.

- In the evaporator 4 500 kg of water are removed ^{from 1m 3 of liquid manure.}

- The amount of processing aid added is neglected.

- The efficiency of the evaporator with vapor compressor is 50% or 0.5.

- There is no condensate storage facility.

The evaporator with vapor compressor is known to represent a form of a heat pump, the maximum performance coefficient pwp of which can be calculated according to equation 3. maximum coefficient of performance

Q Energy required for evaporation

("Supplied heat", "heat pumped into the heat reservoir") w Work performed by the heat pump (= evaporator with vapor compressor)

The work to be calculated, which the evaporator 4 does to form the concentrate, is obtained by transforming equation 3, with a real performance coefficient being used for calculation: real coefficient of performance Q and r | wp _, real are therefore to be calculated.

The energy (heat, Q) required for evaporation can be calculated using the following equation (constant pressure):

From equation 4 it follows for lm ³ liquid manure to evaporate 500kg water:

The real performance coefficient pwp, real can be calculated from the maximum performance coefficient, taking into account the specified efficiency:

Equation 3 is used to calculate the maximum coefficient of performance pwp. At atmospheric pressure, water is known to evaporate at 100 ° C (= 373 Kelvin). The condensation takes place at 90 ° C (= 363 Kelvin), see assumptions made. The following applies:

Substituting result 3 into equation 5 gives:

Substituting results 2 and 4 into equation 3.1 gives after using the evaporator with vapor compressor, 16.8 kW * h of electricity (electrical energy) are required to obtain ^{the concentrate from 1m 3 of} liquid manure. This amount of electrical energy (current) is then equivalent objectified in the concentrate obtained, which thus forms a pseudo energy store.

In order to arrive at the pseudo energy storage density, the volume required for storage must be taken into account. The starting material, namely lm ³ manure, needs a volume of lm ³ . The concentrate requires 0.5 m ³ (lm ³ liquid manure - 500 kg evaporated water). The storage requirement is therefore 1.5 m ³ .

Result 5 and the storage requirement give the pseudo energy storage density:

4.2.2 Regarding the pseudo-energy storage solution potassium hydroxide and phosphoric acid In the following, calculations are carried out on the amount of electricity required for the electrolysis taking place in the electrolysis cell 9. Potash lye and phosphoric acid are formed.

The electrolysis cell 9 is divided into two half-cells - an anode compartment and a cathode compartment - with a membrane permeable ^{to potassium cations (K +).} When a direct current / direct voltage is applied, the potassium cations (K ⁺ ) migrate through the membrane into the cathode compartment and form hydrogen (H2) and potassium hydroxide (KOH) on the cathode, whereby potassium hydroxide is formed. The phosphate anions (PO ₄ ^3- ) migrate into the anode compartment and form phosphoric acid, oxygen and carbon dioxide at the anode.

The following assumptions are made for the calculation:

• The pH value of the eluate is 12. At this pH value, the phosphate anions of the potassium phosphates are available as PO ₄ ^3- , so that the following calculations refer to PO ₄ ^3- . • The voltage difference during electrolysis is 5V. This voltage is above the decomposition voltage.

^{Ultimately, only protons (H +} ) and hydroxide ions (OH) react at the electrodes of the electrolysis cell 9, since these supposedly “migrate” faster in the electric field than the other ions (Grotthuss mechanism).

Three moles of electrons are transferred per mole of potassium phosphate (K3PO4), ie per mole of phosphate anions (PO ₄ ^3-). At the same time, three moles of electrons are transferred to the protons (H ⁺ ). The amount of charge Q required for the conversion of one mole of potassium phosphate results from: q Amount of charge

F Faraday constant (= electrical charge of one mole of a singly charged ion), F = 96,485.33 C / mol

It also applies:

Weiektr = U * q equation 7

W _ectr electrical work when shifting the charge q between two points between which the voltage U exists U voltage (sdifference) q amount of charge

Substituting result 6 into equation 7, we get:

To convert one mole of potassium phosphate (K ₃ PO ₄ ), 0.402 kWh are therefore required (ie 0.402 kWh / mol). This means that to convert one kilogram of potassium phosphate (molar mass = 0.21228 kg / mol) required are.

It is assumed that the present electrolyte solution (eluate) is a 50% potassium phosphate solution. Such has a density of about 1,500 kg / m ³ . For the implementation of 1m ³ potassium phosphate solution are therefore required.

In order to arrive at the pseudo energy storage density, the volume required for storage must be taken into account. The starting material, namely the lm ³ electrolyte solution, requires a volume of lm ³ . The potassium hydroxide solution and the phosphoric acid formed together also take up approx. ¹ ^{m 3} , so that the storage requirement is around 2.0 m 3.

Result 9 and the storage requirement give the pseudo-energy storage density:

The exemplary calculations clearly show that the system according to the invention or the method according to the invention can be used to achieve significantly higher pseudo energy storage densities than with the conventional methods known to date, for example a pumped storage power plant.

List of reference numerals

1 . Slurry storage

2. Mixer

3. Potash lye storage

4, 4 ‘evaporator

5, 5 ‘condensate storage

6, 6 ‘electrolytic cell

7. reactor

8, 8 ‘block-type thermal power station

9. Electrolytic cell

10 ... eluate store

11 ... concentrate storage

12. Biogas plant

S1 to S5 system

Claims

1. Process for energy management with the participation of

- at least one power grid,

- At least one process generating electrical energy, the method being operated as a function of the control energy requirement in one of the following operating states: a) with no control energy requirement in normal operation, in which the electrical energy consuming process is at least one product with the energy of the electrical energy generating process produces, b) if there is a need for negative control energy in a storage operation, in which additional electrical energy is fed into the electrical energy consuming processes from the power grid and in this way an excess of product is produced compared to normal operation and this is stored and c) if positive control energy is required in a delivery operation in which the energy-consuming process is shut down or throttled and the electrical energy of the electrical energy-generating process is fed into the power grid.

2. The method according to claim 1, characterized in that the product or the

Products, which or which with the electrical energy consuming

Process is or are produced, is or are liquid or gaseous.

3. The method according to claim 1 or 2, characterized in that a product or products is or are manufactured with the electrical energy consuming process which can be stored in a stable manner without additional energy expenditure, such as cooling .

4. The method according to any one of claims 1 to 3, characterized in that the electrical energy consuming process is an electrolysis process, in particular an electrochemical membrane process, a metal extraction electrolysis, an electrochemical cleaning of metals, a process falling under the term of electroplating, an organic electrosynthesis or is a water electrolysis.

5. The method according to any one of claims 1 to 4, characterized in that the electrical energy consuming process is an evaporation of water from water-containing starting materials.

6. The method according to any one of claims 1 to 5, characterized in that at least one product is produced by means of the electrical energy consuming process, which is at least partially used as starting material for the electrical energy generating process.

7. The method according to any one of claims 1 to 6, characterized in that at least one water-containing biological starting material, in particular a biogenic raw material or a biogenic residue, is used for the electrical energy consuming process, preferably organic waste or wastewater as the biogenic residue, the biogenic portion that occurs during mechanical-biological waste treatment, agricultural and forestry by-products, biogenic production residues, liquid manure, fermentation residues from a biogas plant, sewage sludge, slaughterhouse waste, animal meal, residual forest wood, residues from forest and wood industrial production, landscape maintenance material, waste from gardens, parks and cemeteries, organic waste, excrement from animal husbandry and / or greenery along the road is or are used.

8. The method according to any one of claims 1 to 7, characterized in that several processes consuming electrical energy, in particular at least one evaporation and at least one electrolysis process, preferably an electrochemical membrane process, are involved.

9. The method according to any one of claims 1 to 8, characterized in that the power network involved is an interconnected network.

10. The method according to any one of claims 1 to 9, characterized in that the electrical energy consuming process runs continuously in normal operation.

11. The method according to any one of claims 1 to 10, characterized in that the electrical energy consuming processes comprise the following successive steps: i. Mixing a biological starting material containing organic compounds and water with an alkaline hydrolysis agent dissolved in water to form a hydrolyzed medium, ii. Heating and evaporation of the hydrolyzed medium to form a vapor and a concentrate, iii. a) in normal operation: use of the concentrate to generate electrical energy by means of the electrical energy-generating process, b) in storage mode: use of a partial amount of the concentrate to generate electrical energy by means of the electrical energy-generating process and storage of the further concentrate, c) in the dispensing operation : Use of the concentrate stored in the storage facility to generate electrical energy by means of the electrical energy generating process.

12. The method according to claim 11, characterized in that the in step i. used hydrolysis agents at least one from the group sodium hydroxide, sodium carbonate, sodium hydrogen carbonate, lithium hydroxide,

Lithium carbonate, lithium hydrogen carbonate, potassium hydroxide, potassium carbonate, potassium phosphate, potassium hydrogen phosphate, potassium dihydrogen phosphate or dipotassium hydrogen phosphate.

13. The method according to claim 11 or 12, characterized in that the in step ii. accumulating vapors are condensed and converted into an ammonia solution with the addition of at least one acidic process auxiliary in at least one electrolysis cell (6).

14. The method according to any one of claims 11 to 13, characterized in that in step iii. the concentrate for generating electrical energy is heated in a reactor (7) to up to 700 ° C and the resulting gases are converted in a block-type thermal power station.

15. The method according to claim 14, characterized in that the in step iii. residue remaining in the reactor is mixed with water to form an eluate, with at least part of the eluate after separation of the ash in an electrolysis cell one for step i. suitable hydrolysis agent is formed.

16. The method according to any one of claims 1 to 10, characterized in that the electrical energy consuming processes comprise the following successive steps:

I. Evaporation of a biological starting material containing organic compounds and water to form a vapor and a concentrate, II. A) in normal operation: converting the concentrate in a

Biogas plant (12), whereby a digestate is formed and this is discharged from the biogas plant (12), b) in storage mode: Feeding in electrical energy in step I, so that an excess of concentrate is formed, which is then stored in the biogas plant (12) c) in the delivery operation: formation of biogas from the concentrate stored in the storage operation and generation of electrical energy from the biogas.

17. Comprehensive energy management system

- at least one power grid,

- At least one first system component (8, 8 ‘) for generating electrical energy,

- At least one second system component (4, 4 ‘, 6, 6‘, 9) for producing at least one product using electrical energy of the first system component (8, 8 ‘),

- At least one store (3, 5, 10, 11) for storing excess product and

- An electronic control system, which feeds electrical energy from the power grid into the second system component (4, 4 ', 6, 6', 9) when the control energy is negative and the supply of electrical energy from the first system component (8, 8 ') when the control energy is positive. ) throttles or switches off in the second system component (4, 4 ', 6, 6', 9) and at least partially feeds the electrical energy generated in the first system component (8, 8 ') into the power grid.

18. System according to claim 17, characterized in that there are a plurality of first system components (8, 8 ') and / or a plurality of second

System components (4, 4 ', 6, 6', 9) includes.

19. System according to claim 17 or 18, characterized in that a first system component (8, 8 ‘) is a combined heat and power unit (8, 8‘).

20. System according to one of claims 17 to 19, characterized in that one or more second system component (s) (4, 4 ', 6, 6', 9) is or are provided, which an evaporator (4, 4 ' ), an electrolysis cell (6, 6 ', 9) and / or a biogas plant (12) is or are.