WO2012110325A1

WO2012110325A1 - Method and reactor for hydrothermal carbonization of biomass

Info

Publication number: WO2012110325A1
Application number: PCT/EP2012/051824
Authority: WO
Inventors: Bernd Utz; Marco Dornauer
Original assignee: Siemens Aktiengesellschaft
Priority date: 2011-02-18
Filing date: 2012-02-03
Publication date: 2012-08-23
Also published as: DE102011004398A1

Abstract

The invention relates to a method for hydrothermal carbonization, in which biomass (3) is fed to a reactor (1') and is excited to undergo a chemical reaction, after which reaction products (13, 15, 29, 29a, 29b, 29c, 29d,..., 29n) are taken from the reactor (1'). The biomass (3) is fed and/or the reaction products (13, 15, 29, 29a, 29b, 29c, 29d,..., 29n) are removed during ongoing reaction operation in the reactor (1'). The invention also relates to a reactor (1') for implementing such a method.

Description

description

Process and reactor for the hydrothermal carbonization of biomass

The present invention relates to a method for

hydrothermal carbonization, in which biomass is fed into a reactor and excited to a chemical reaction and then reaction products are removed from the reactor. It also relates to a reactor for such hydrothermal carbonization of biomass.

Hydrothermal carbonation is a chemical process for the simple and efficient production of

Reaction products such as lignite, synthesis gas, liquid petroleum precursors and humus or peat from biomass under

Release of energy. Ultimately, this process reflects the nature of lignite, which occurs in nature in 50,000 to 50 million years, with the difference that the reaction takes place within a few hours.

Such a method is shown below with reference to Figure 1: Biomass 3 is first crushed in a treatment tank 6 and together with reaction water 5 and a reaction support means 7, namely a

Catalyst, here citric acid, placed in a reactor 1. At the beginning of the process heat ΔΤΊ _{η is} supplied, whereby an endothermic reaction is initiated. This leads to an endothermic reaction in which bound water is separated from the biomass and heat AT _out arises. Gases 9, such as CO 2 and water vapor are removed during the process. After about 12 hours, practically only carbon, in the form of a lignite-like suspension, is present. About a pipe 11 is this

Reaction product transferred to a first dryer 31, where a mechanical drying, here by centrifuging, is performed. Waste water 13 is discharged from the dryer 31, while the now pre-dried Reaction product is forwarded to a second dryer 33. In the second dryer 33 is a thermal

Drying by the addition of heat AT _dry and removal of water vapor 15. The final reaction product 29 is a dry, granular, lignite-like substance.

The biomass 3 is in particular to

vegetable material, its organic constituents

simplified with the formula of sugar

can be rewritten. The reactor 1 is a pressure vessel whose

Interior volume is not changed during the reaction.

The reaction produces not only waste heat AT _out , but also a significantly increased pressure, which can be up to 2 MPA. During the reaction, oxonium ions are formed which lower the pH to 5 and below. This effect can be anticipated by adding reaction promoting agents such as citric acid 7 as a catalyst. It should be noted that the lower the pH, the more

Carbon goes into the aqueous phase.

The end of the reaction is reached when 90 to 99% of the

Carbon dissolved as an aqueous sludge from

Brown coal spheres (formula C ₆ H ₂ O) with pore sizes between 8 and 20 nm are present as a solid phase. The remaining 1 to 10% of the carbon is either dissolved in the aqueous phase or converted to carbon dioxide.

The reaction equation is approximate

C ₆ Hi ₂ 0 ₆ -> C ₆ H ₂ 0 + 5H ₂ 0.

The reaction liberates 1105 kJ of energy per mole.

This reaction can be stopped prematurely, that is, with still incomplete elimination of water from the

Biomass 3, where you get depending on the previous reaction time different intermediates. After a few

Minutes already arise liquid intermediates, lipophilic substances whose handling would, however, be very difficult to control because of their high reactivity. Subsequently, these substances polymerize, and peat-like structures are formed, which are present after about 8 hours as intermediates. After that arise the above

mentioned lignite-like substances and later still hard coal-like substances.

In the previously known methods for hydrothermal

Carbonation is a smaller scale application because the process is difficult to control and requires many preparatory steps such as coarse sorting and size reduction as well as post-processing steps (especially drying and reactor 1 purification). In addition, the process currently proves to be relatively cumbersome, since in each case for filling and emptying and cleaning of the reactor 1 working rush hours arise, while then incurred in the entire course of the 12 hours of the reaction hardly any further work. At the same time, the process can only be automated inadequately.

The object of the invention is therefore to enable an improved, in particular preferred, a process simplified in the course of hydrothermal carbonization and to provide the corresponding working means therefor. Another optional object of the invention is to effectively reuse the resulting reaction products.

This object is achieved by a method according to claim 1 and by a reactor according to claim 12.

Accordingly, in a method of the type mentioned according to the invention, a supply of biomass and / or removal of the reaction products during an ongoing reaction operation in the reactor. The invention thus turns away from strictly discontinuous operation and instead realizes a quasi-continuous

Reaction process. Here are in the current reactor operation Biomass supplied or reaction products

taken. Particularly preferably, both - both the supply of biomass and the removal of

Reaction products - during reactor operation. Such a simple and effective procedure also makes it possible

Waste heat generated during the phase of the exothermic reaction, for heating in the context of a parallel endothermic reaction in the context of a return

to reuse. This creates a heat cycle in which only minimal energy must be supplied in order to obtain the desired reaction products from the biomass

win. The quasi-continuous realization of the

Procedure also requires that the reactor does not have to be switched on and off again and again, but can be operated constantly, and the peak times of the workload for the operation of the reactor can be at least reduced. In other words, both the working and the

Energy use minimized and the operating time of the reactor optimally utilized to a maximum yield of the

To enable reactor. In addition, it is possible to obtain reaction products from the reactor at relatively regular and narrow intervals, for example in order to process them further industrially or to use them energetically.

Vegetable material is preferably used as biomass, but it is also possible to use animal substances or other biological material, for example fungi. Furthermore, the term biomass in the

present case also plastics with simple

Hydrocarbon compounds such as polyethylene. In fact, such substances can also be used in the context of the process since they too can be converted into similar or identical reaction products as the biomass generated from biological processes.

According to a particularly preferred embodiment of the invention

The process according to the invention is carried out in a pre-reactor, in which also carried out an initial reaction becomes. The pre-reactor is spatially separated at least during the feed from a main reactor in which an exothermic chemical reaction is carried out. The reactor is thus in at least two different

Subdivided reaction chambers, of which the first, namely the pre-reactor, is used as an atrium. The pressure built up in the prereactor in the course of the reaction and the temperature achieved there can be transferred to the main reactor, so that the pressure and temperature conditions are essentially the same in both reactor parts.

Due to the separation in the pre- and main reactor, it is possible to separate the execution of the endothermic reaction functionally and spatially from the execution of the exothermic reaction and to perform in different chambers. This also means that the feed of the reactor, that is, the supply of biomass in the prereactor can be completely independent of the operation of the main reactor, and vice versa, the emptying of the main reactor completely

independent of the operation of the reaction in the prereactor

can be carried out.

The result is a workflow in which two out of four sub-processes within the workflow are executed completely independently of each other. These four

Partial processes are: The loading of the reactor with biomass, the initial endothermic reaction, the exothermic reaction and the discharge of the reactor. So it's possible

to load at the same time and the exothermic reaction

to run simultaneously to run the endothermic and the exothermic reaction or simultaneously perform the endothermic reaction and a discharge of the reaction.

Accordingly, an inventive reactor of the type mentioned is formed. He includes one

Pre-reactor and a at least temporarily separated from the prereactor main reactor as reactor parts, wherein the two reactor parts are formed together so that in one ongoing reaction operation, a feed of the biomass into the prereactor and / or a removal of reaction products from the main reactor can be carried out without the

Reaction operation in the other part of the reactor to

interrupt. The delivery of biomass, i. the loading and / or unloading, i. the removal of

Reaction products are preferably controlled by a suitable control device, which particularly preferably derives control commands for at least one of these two processes from a time control and / or from user commands. This can ensure that the reactor

coordinated and / or (partially) emptied in a timely and / or demand-oriented manner.

Further particularly advantageous embodiments and

Further developments of the invention will become apparent from the dependent claims and the following description. In this case, the method according to the invention can also be developed according to the dependent claims to the reactor and vice versa.

Preferably, the biomass is heated in the prereactor and

particularly preferably by feeding

Reaction assistants to a target pH

brought. This means that the pre-reactor serves to initiate the reaction of the hydrothermal carbonization, that is, the biomass on a

To bring energy level, from which exothermic

Carbonation reaction takes place. In other words, the pre-reactor is the part of the reactor in which the carbonation reaction is initiated until it becomes self-contained

continues. In the main reactor, this autonomous reaction is then continued without another

Heat supply and thus a heater in

Main reactor would be necessary. The target pH may be considered to be pH 5 and below.

Reaction supportive agents are on the one hand

Reaction water, which in particular during the reaction in the pre-reactor acts as a carrier and transfer agent and on the other hand, catalysts or acids, such as the above-mentioned citric acid, which serve to reduce the pH. It has proven to be particularly advantageous to use such a main reactor, which is divided into at least a first part-reactor and an end-part-reactor, which are temporarily separated from each other. The main reactor is thus in several reactor chambers or partial reactors

subdivided, which are preferably arranged vertically above one another, wherein the partial reactor having the respective lower order number above the partial reactor with the

is positioned next higher order number. As a result, the reaction intermediates formed in the respective partial reactors can be forwarded to the next partial reactor by utilizing gravity.

The partial reactors are temporarily separated from one another, which means that individual reaction steps take place in the partial reactors, without any connection to the other partial reactors. The result is that in each of the sub-reactors a separate category of reaction intermediate (or fraction) can be prepared separately and then, if necessary, after expiration of one of these

provided reaction time is transferred to the next part of the reactor. On the other hand, there is a need for a reaction intermediate, which arises before the

Carbonization process is completed, so this intermediate reaction product can be obtained directly from the respective partial reactor by removal. Thus, for example, humus or peat can be removed from the circulation in order to distribute it as a fertilizer instead of a completely completed carbonization to brown coal. The partial reactors can also be seen as a kind of "indulgence" in which the

Reaction continues for a certain period of time, before the reaction mixture reaches the next level of inactivity. Preferably, the main reactor comprises at least three partial reactors, more preferably even four partial reactors. In general, the increase in the number of partial reactors can lead to a differentiation of the reaction process in that very different

Reaction products can be produced and removed if necessary. In addition, the increase in the number of sub-reactors can also be used to optimize the timing of the process: it takes about eight hours to form peat, while only four hours are required to then produce lignite from this. It may therefore be advantageous to use two sub-reactors, with only the second complete peat being present, while the piling process is only begun in the first of the two sub-reactors. After four hours, the intermediate reaction product is then passed from the first peat-part reactor to the second peat-part reactor, and after a further four hours, passed into another partial reactor in which lignite is produced. This results in a clocking of four hours, compared to a clock of eight hours, when peat in one

individual partial reactor is formed. This eliminates idle times in the fractional reactor where lignite is produced.

The subdivision of the main reactor into several sub-reactors can be seen analogously to the separation process in a refinery, in which as well as here partial products or

Fractions arise. One could therefore call the intermediate reaction products and the final reaction products each as fractions. However, there is the striking

The difference is that in a refining process substances are essentially separated from one another by physical methods (heating and use of different densities) and these substances are present in the starting material (petroleum) right from the outset. In an inventive

Reactor, however, the production of the substances to be separated takes place only on site. This means that from the initial product biomass the end products such as humus, lignite-like Substances or the like can not be derived immediately, but only be formed by chemical reaction.

In addition, the separation is carried out in the process according to the invention essentially by two combined

Principles: Firstly, in the multi-chamber system in the

Main reactor no substances separated from each other, but mixtures of substances with certain chemical properties

Temporarily separated from each other and second, it depends on the right timing, when certain substances that

Reaction cycle are taken or when they are forwarded to the next chamber. Accordingly, the reactor is preferably equipped or connected to a control device which, in operation, depends on a (reaction) given in accordance with a rule.

times a discharge and / or forwarding of intermediate reaction products abuts.

The biomass and / or by reaction from the biomass

recovered intermediate reaction products are preferably from the prereactor in the main reactor and / or from one part-reactor to a next part-reactor via sluices and / or

Valves forwarded. Such locks, such as rotary valves, or such valves are used, controlled and possibly differentiated metered the biomass

or to be able to forward from it resulting reaction intermediates or end products. This also means that not the complete content of the pre-reactor or partial reactors must be passed on at once, but it can also be a partial transmission.

For example, thereby the other part, which was not forwarded, remain still in a particular part-reactor or discharged to the outside and one

be used elsewhere.

Accordingly, this is also provided that before removal of end reaction products, ie, for example

lignite or coal-like substances, from the end-part reactor intermediate reaction products such as petroleum precursors, humus, or lignite-like substances are removed from a partial reactor, which is arranged in the main reactor in the process direction before the end-part reactor.

Such "premature" removal of intermediate reaction products takes place as already mentioned above as needed. For example, may be seasonal, about in

In the spring, in a field of application of the reactor there is a need for humus to improve or fertilize soils, while in autumn and winter, for example, the demand for fuel tends to increase. However, there may also be a need for different usable products, which will be served depending on the market situation. The advantage in the removal of intermediate reaction products is thus to be seen in that it can be flexibly responded to market requirements and technical requirements and thus not only a reaction end product, but a variety of different reaction products can be provided.

Special advantages arise in the context of the process, if in the first part of a reactor reaction to

Presence of aqueous petroleum precursors and / or in a second sub-reactor a reaction to the presence of humus or peat and / or in a third part of the reactor, a reaction to the presence of reaction products which have substantially substance properties of lignite , is carried out. This part-reactor, which supplies lignite-like substances, is according to a preferred

From the embodiment of the invention, the end-part reactor, or, in other words, in the end-part reactor, the reaction is continued until the presence of brown coal-like products.

Conducting the reaction until certain predefined and well - known classes of

Reaction products in a sufficiently high concentration thus requires a functional separation of the partial reactors from each other. So you could also say that the the first part-reactor acts as a "crude oil precursor reactor", the second part-reactor as a "humus reactor" and the third part-reactor as a "brown coal reactor". Such a designation and functional assignment can advantageously be displayed directly on the outside of the respective sub-reactors in order to present even unknowable users, which products can be obtained from the respective sub-reactor after expiration of the reaction time provided for this purpose.

Special effects result from the combination of the reaction products generated in the process of the invention in the field of power plant technology. Due to the quasi-continuous production process is also a quasi-continuous supply of fuel for ^¬

thermal power plants possible. This results

considerable advantages in the operation of combustion power plant area, since now practically uninterrupted fuel

which can then be used directly to generate biomass electricity. It will therefore

preferred that reaction products from the method according to the invention for firing a power plant for the generation of electric power are forwarded. These

Reaction products can be directly via piping

or conveyor belts are transported from the reactor to the power plant.

A reactor according to the invention is therefore preferably developed in such a way that it has a compound for the transmission of the reaction products to a power plant for the production of

includes electric power, so that the reaction products can continue to be used for firing the power plant. Such a compound is in effect a transport compound for the reaction products and can be both standing

Connection, for example in the form of a pipeline to be realized as well as a temporary transport connection, for example, realized by other terrestrial means of transport. Such means of transport may include, inter alia Trains or trucks act on a Schienenbzw. Road connection from the reactor to the power station.

Particularly suitable is the use of the reaction products from the inventive method for supporting firing in a heating circuit, in particular in a solar thermal power plant. While conventional heating plants, the

For example, be fired with fossil fuels, always produce enough heat to drive turbines and generate electricity, solar thermal power plants require a so-called back-up firing, which is mainly used when not enough heat through

Solar radiation is generated on the solar field of the power plant. Such support firing is also necessary in arid regions, for example, when clouds follow the path of the

To obstruct or block sun rays on the solar field

Twilight or night. For such cases, it is therefore currently usually necessary for a long time

Transport connections (using pipelines or

Land transport) to transport fossil fuels to the power plant. Alternatively, the local reference of regenerative, i. of course, renewable, seen as fuel wood. Especially in arid zones, however, there is not enough wood or other flammable substances that could be extracted from local agricultural or forestry cultivation. There is therefore currently a dilemma between the effective use of solar energy, which is known to be particularly prevalent in desert and steppe regions

abundant, and the practical impossibility of regenerative support firing, as any crop cultivation must primarily serve the food supply in the region. A solution based entirely on regenerative energy sources for solar thermal power plants was therefore only possible in exceptional cases so far.

Due to the improvements by the invention

Method is now the use of biomass via the detour of the hydrothermal carbonization a simple, inexpensive and viable alternative to using wood products. This will be local land or

In addition, forestry resources are spared and, in addition, power generation at the power plant is based solely on sustainable energy sources. Also, using the

hydrothermal carbonation a concentration of

Calorific value compared to biomass and also produces an inert fuel that is much easier to store than the biomass itself.

The end effect is thus a cycle in which a local solar thermal power plant, supported by

Supporting products that are produced indirectly from the local

Agriculture provides energy that in turn can be used in whole or in part to support local agricultural cultivation.

The invention thus also includes a power plant, in particular a solar thermal power plant comprising a

Main heat energy source and a Stützfeuerung with a compound as a feed line for reaction products prepared by a method according to the invention. In the

Main heat energy source is preferably a solar panel with a number of solar panels, the

Solar radiation generate heat. This heat is then used in a heating circuit to directly or indirectly drive a turbine to generate electricity.

As it is particularly advantageous, as explained above, a kind of local association of agricultural production,

Implementation of biomass, hydrothermal carbonization and solar thermal power production to realize the invention relates in effect also a power plant-reactor complex comprising a reactor according to the invention and a

according to the invention of the power plant, which are functionally linked to each other in a local, that is local composite, that the reactor provides the power plant reaction products for feeding the auxiliary firing. The definition of "Local" in this context depends essentially on the catchment area of the power plant and / or the reactor: It is therefore defined by the reference area for the biomass on the one hand and the power station current on the other hand, where

preferably in each case the further reference area is still rated as "local".

In the context of the combination of inventive reactor and inventive power plant, however, it is particularly

advantageous because effective when the power plant in

is operated in close proximity to the reactor. Particularly preferably, the reactor and the power plant are subunits of a production plant, which are preferably arranged on a common operating area. This results in very short connections; a simple control of the processes, in particular the

integrated processes is possible, and there is little loss of operating material and heat.

Finally, the invention comprises a method for operating a power plant, preferably a solar thermal

Power plant, in which by means of an inventive

Process produced reaction; used for firing power station.

Energetically very effective and therefore special

It is advantageous if coal-like reaction products, ie lignite or coal-carbon reaction products, are forwarded to the power plant. These reaction products have a particularly high calorific value; their drying out of the aqueous solution can also be achieved by using residual heat from the reaction process or from the heating and / or

Operating cycle of the power plant to be performed.

The invention is described below with reference to the

attached figures explained in more detail by means of embodiments. There are in the different Figures identical components provided with identical reference numerals. Show it:

1 shows a schematic block diagram of the principle of a hydrothermal carbonization according to the prior art,

Figure 2 is a schematic block diagram of a

Embodiment of a reactor according to the invention for carrying out a novel inventive

Carbonization process,

Figure 3 is a schematic block diagram of a

Embodiment of a power plant reactor complex according to the invention.

Figure 1 has already been explained above in the context of the description of the prior art.

Figure 2 shows an embodiment of a reactor according to the invention 1 'with a pre-reactor 17 and a main reactor 19, which are connected to each other via a lock 21. In the prereactor 17, biomass 3, in particular vegetable biomass, together with water of reaction 5 and citric acid 7 is fed. The biomass 3 is, as already explained in connection with Figure 1, crushed. By means of a

Heating element 27, here a heat exchanger 27, the mixture in the prereactor 17 is heated so that initially an endothermic Karbonisierungsreaktion is started.

The main reactor 19 is divided into n sub-reactors 25a, 25b, 25c, 25d, ..., 25n. In the main reactor 19 is followed by the endothermic reaction independent running exothermic Karbonisierungsreaktion of related from the prereactor 17 mixture with release of exhaust gases 22, namely carbon dioxide and steam. Thus, a reaction can take place in the first part-reactor 25a, as a result of which

Intermediate 29a, for example in the form of one

aqueous petroleum precursor is present. In the second partial reactor 25b the reaction can continue until a second one

Intermediate 29b, for example as humus

or peat present. In the third partial reactor 25c, the reaction is carried out to a third intermediate product 29c, such as a lignite-like substance, and in the fourth partial reactor 25d, the mixture reacts further until the

Presence of a fourth intermediate or final product 29d, for example in the form of a charcoal-like substance. All the mentioned intermediate or end products 29a, 29b, 29c, 29d are mixed with the water of reaction or the water which is deposited during the reaction. In total, an intermediate or end product 29a, 29b, 29c, 29d, 29n can be obtained in each of the n partial reactors 25a, 25b, 25c, 25d,... 25n. An end product 29n may be, for example

Include slags and other sediments. The sub-reactors 25a, 25b, 25c, 25d, 25n are arranged in the order of their mention from top to bottom and separated by separators 24a, 24b, 24c, 24n. Via valves 23a, 23b, 23c, 23n, the intermediate and final reaction products 29a, 29b, 29c, 29d, 29n can be introduced both into the respective next sub-reactor 25b, 25c, 25d, 25n

be forwarded as well as discharged if necessary for removal to the outside. In the valves 23a, 23b, 23c,

23n are therefore three-way valves 23a, 23b, 23c, 23n. The forwarding or removal of the reaction

Intermediate or end products 29a, 29b, 29c, 29d, 29n on the basis of control commands SB, which consists of a

Control unit 26 are related. This control unit 26 receives user commands NB and Timing commands Tim via suitable interfaces (not shown) to go to the right

Time, that is, in each case after the expiration of a reaction time in which the above reaction intermediate or

End products 29a, 29b, 29c, 29d, 29n are present, a

Forwarding or removal of these products 29a, 29b, 29c, 29d, 29n make. The user commands NB refer to a reference request for certain

Reaction products 29a, 29b, 29c, 29d, 29n and may each according to current product needs, for example a need for humus 29b for fertilizing fields.

A particularly preferred application of the reactor 1 'according to the invention is shown in FIG. 3 for use in a power plant-reactor complex 65. Here, the reactor 1 'is disposed within a reactor complex 61 and

combined with a solar thermal power plant 63. The

Reactor complex 61 comprises in addition to the reactor 1 'a

Preparation tank 6, a first dryer 31, a second dryer 33 (see Figure 1), a silo 35 and a connection 36 in the direction of the power plant 63, which is realized as a supply line in the power plant 63. As already in the context of the description with reference to FIGS. 1 and 2

described the biomass 3 on the

Treatment tank 6 fed into the reactor 1 'and reaction products 29 forwarded from the reaction described in more detail in connection with Figure 2 in the first dryer 31 for mechanical drying and then in the second dryer 33 for thermal drying. The product dried in this way, for example brown or hard coal in the form of granules, is collected and stored in the silo 35 and, if necessary, passed on to the power plant 63 via the line connection 36.

The power plant 63 comprises a solar field 39 with a plurality of solar panels, which is arranged in a cardiovascular 45. A carrier medium, here oil, is circulated in the heating circuit 45 via a pump 43, heated in the solar field 39 and

optionally additionally brought to a target temperature via a Stützfeuerung 37. In an evaporator 41, the temperature of the oil is used to make water in one

Operating cycle 47 to heat so that it produces water vapor. The operating circuit 47 is operated by means of a second pump 49, so that after passing through the

Evaporator 41 generated steam drives a turbine 53, which in turn operates a generator 55. Of the

Generator 55 generates from the rotational energy of the turbine 53 electricity. In a condenser 51, which is connected to a cooling tower 57, the water vapor is cooled again to a lower temperature, so that in

Extending direction V behind the capacitor 51 in

Operating cycle 47 again water is present.

The Stützfeuerung 37 serves to provide the additional heating power that can not be provided by the irradiation of the sun 59 to the solar panel 39 at a certain time. This is the case, for example, when the sun is cloudy or at dusk or night. In such cases, the Stützfeuerung 37 wholly or partially assumes the function of heat generation to ensure the necessary operating temperature of the heating circuit 45.

The power plant-reactor complex 65 is located on an area on which the reactor complex 61 and the power plant 63 are located in common. This results in a direct feed of the biomass 3 obtained

Reaction products 29 in the power plant 63. The electrical energy that can be obtained from the power plant 63, in the sequence, for example, for the operation

agricultural equipment and production units (not shown). These production units can in turn deliver biomass 3 for the operation of the reactor 1 '. This creates a closed energy and

Product cycle, which is also used to develop local

Agriculture and energy production can be used.

It is finally pointed out again that it is in the previously described in detail methods and in the illustrated reactor or power plant or

Power plant reactor complex only to exemplary embodiments, which the expert in a variety of ways

can be modified without departing from the scope of the invention. Furthermore, the use of the indefinite article "on" or "one" does not exclude that the characteristics in question may also be present multiple times. In addition, you can "Units" consist of one or more, also spatially distributed components.

Claims

claims

1. A process for hydrothermal carbonization, in which

Biomass (3) is fed into a reactor (1 ') and is excited to a chemical reaction and thereafter

Reaction products (13, 15, 29, 29a, 29b, 29c, 29d, 29n) are taken from the reactor (1 '), wherein a feed of the biomass (3) and / or removal of the reaction products (13, 15, 29, 29a , 29b, 29c, 29d, 29n) during an ongoing reaction operation in the reactor (1 ') takes place.

2. The method according to claim 1, wherein the feed into a pre-reactor (17) takes place, in which an initial reaction is carried out, wherein the pre-reactor (17) spatially separated at least during the supply of a main reactor (19), in which an exothermic chemical reaction is performed.

3. The method according to claim 2, wherein the biomass (3) in the prereactor (17) is heated and preferably brought by supplying reaction support means (5, 7) to a target pH.

4. The method according to claim 2 or 3, wherein a main reactor (19) is used, which is divided into at least a first partial reactor (25a) and an end-part reactor (25n), which are temporarily separated from each other.

5. The method according to any one of claims 2 to 4, wherein the biomass (3) and / or by reaction from the biomass (3) obtained intermediate reaction products (29a, 29b, 29c, 29d) from the pre-reactor (17) in the main reactor ( 19) and / or from a partial reactor (25a, 25b, 25c, 25d, ...) in a next partial reactor (25b, 25c, 25d, 25n) via locks (21) and / or valves (23a, 23b, 23c, 23n).

6. The method according to any one of claims 4 or 5, wherein prior to removal of end reaction products (29n) from the final Partial reactor (25n) intermediate reaction products (29a, 29b, 29c, 29d) are taken from a partial reactor (25a, 25b, 25c, 25d) in the main reactor (19) before the end-part reactor (25n ) is arranged.

A process according to any one of claims 4 to 6, wherein in the first part-reactor (25a) a reaction until the presence of aqueous petroleum precursors (29a) and / or in a second part-reactor (25b) a reaction until Presence of humus (29b) and / or in a third part-reactor (25c), a

Reaction until the presence of reaction products (29c), which have substantially substance properties of lignite, is carried out.

8. The method according to any one of the preceding claims, wherein reaction products (29, 29a, 29b, 29c, 29d, 29n) for

Firing a power plant (63) to produce

electric power to be forwarded.

A method according to claim 8, wherein the reaction products (29, 29a, 29b, 29c, 29d, 29n) in a solar thermal power plant (63) are used in a support furnace (37) in the heating circuit (45).

10. The method according to claim 8 or 9, wherein coal-like reaction products (29, 29c, 29d) are forwarded to the power plant (63).

11. A method for operating a power plant, preferably a solar thermal power plant (63), in which by means of a

Method according to one of the preceding claims

prepared reaction products (29, 29a, 29b, 29c, 29d,

29n) are used to fire the power plant (63).

12. Reactor (1 ') for the hydrothermal carbonization of

Biomass (3) comprising a prereactor (17) and at least temporarily separated from the prereactor (17)

Main reactor (19) as reactor parts (17, 19), wherein the both reactor parts (17, 19) are jointly designed so that in a current reaction mode, a supply of biomass (3) in the prereactor (17) and / or removal of reaction products (29, 29a, 29b, 29c, 29d, 29n) can be carried out from the main reactor (19) without the

Reaction operation in the other part of the reactor (17, 19) to interrupt.

13. Reactor (1 ') according to claim 12, comprising a compound (36) for transferring the reaction products (29, 29a, 29b,

29c, 29d, 29n) to a power plant (63) for generating electric power, so that the reaction products (29, 29a, 29b, 29c, 29d, 29n) for firing the power plant (29, 29a, 29b, 29c, 29d, 29n) can be used.

14 power plant (63), in particular solar thermal power plant (63) comprising a main heat energy source and a

Supporting furnace (37) with a connection (36) as a feed line for reaction products (29, 29a, 29b, 29c, 29d, 29n) produced by a process according to one of claims 1 to 10.

15 power plant-reactor complex (65) comprising a reactor (1 ') according to claim 12 or 13 and a power plant (63) according to claim 14, which are functionally linked to each other in a local composite, that the reactor (1') the

Power Plant (63) provides reaction products (29, 29a, 29b, 29c, 29d, 29n) for feeding the auxiliary firing.