WO2011104259A1

WO2011104259A1 - Method and system for hydrothermally carbonizing biomass and carbon-containing product from the method

Info

Publication number: WO2011104259A1
Application number: PCT/EP2011/052652
Authority: WO
Inventors: Robert Stöcklinger
Original assignee: G+R Technology Group Ag
Priority date: 2010-02-26
Filing date: 2011-02-23
Publication date: 2011-09-01
Also published as: DE102010000576A1; DE102010000576B4

Abstract

The invention relates to a system (1) and method for producing carbon-containing products from biomass (5₁, 5₂,..., 5_n) by means of hydrothermal carbonizing. In a first region (100), at least one type of biomass 5₁, 5₂,..., 5_n) is provided. In a second region (200), the mixed biomass (5M) is treated and prepared. In a third region (300), the reaction process takes place in accordance with hydrothermal carbonizing. In a fourth region (400), the reaction products are further processed. At least three reactors (301) are provided in the third region (300), wherein at least one reactor (301) is always the active reactor (301A). The biomass undergoing the reaction process can be recirculated in a controlled and selective manner by means of a pump via a second heat exchanger (320). For assistance, a stirrer (350) is provided in each reactor (301).

Description

APPARATUS AND METHOD FOR HYDROTHERMAL

CARBONIZATION OF BIOMASS AND CARBONATED PRODUCT FROM THE PROCESS

The present invention relates to a plant for the production of carbonaceous products from biomass by means of hydrothermal carbonization.

The plant for the production of carbonaceous products from biomass comprises a first area in which the supply, crushing and mixing of at least one type of biomass is carried out. In a second area, the preparation and processing of the mixed biomass takes place. In a third area, the reaction process is carried out according to the hydrothermal carbonization. In a fourth area, the further processing of the reaction products of the reaction process takes place.

Furthermore, the invention relates to a method for the production of carbonaceous products from biomass by means of the reaction process of the hydrothermal carbonization.

In the past, many efforts have been made to mimic the natural conversion of biomass to coal. This transformation runs on a time scale of a few hundred to several hundred million years. In the production of charcoal there is already the process of hydrothermal carbonation (HTC). The first experiments on this were already carried out in 1913 by Bergius, who described the conversion of cellulose into coal-like material by hydrothermal transformation. First more systematic investigations were later reported by E. Behrl et al. (Ann. Chem. 493 (1932), pp. 97-123; Angew. Chemistry 45 (1932), pp. 517-519) and JP Schuhmacher et al. (Fuel, 39 (1960), pp. 223-234). In the recent past, the process of hydrothermal carbonation has regained more and more importance and attention. For this, the publications of Q. Wang et al., Carbon 39 (2001), pp. 221 1 -2214 and the publication of X. San and Y. Li, Angew. Chem. Int. Ed. 43 (2004), pp. 597-601).

International Patent Application WO 2010/006881 A1 describes a method for producing a hybrid material from hydrothermal carbonization of biomass. For this purpose, a reaction mixture is first heated. The reaction mixture comprises water, biomass and a copolymerizable substance. The copolymerizable substance is supplied in the preparation of the reaction mixture. From a mixing unit, the reaction mixture is transferred to a reactor. The reaction takes place at a temperature of 190 ° C to 270 ° C from. From the reactor, the biomass is transferred via a heat exchanger in another reactor in which takes place the copolymerization reaction.

German Offenlegungsschrift DE 10 2007 062 810 A1 relates to a plant for the production of energy from biomass, with at least one device for the treatment of the biomass. The device for treating the biomass comprises at least one reactor for receiving the biomass and / or at least one device for processing the biomass and / or for working up the reaction products and / or by-products. The arrangement for power generation preferably comprises a pellet stove, a fuel cell or a power plant with pulverized coal firing, in particular with a pressure-charged stationary fluidized bed firing, particularly preferably with pressurized coal firing.

German Offenlegungsschrift DE 10 2008 026 991 A1 relates to a process for producing coal, in particular coal sludge from biomass, in particular sewage sludge by hydrothermal carbonization. The carbon structures of the biomass are added broken at least 180 ° C to 200 ° C under exclusion of air. Before the hydrothermal carbonization, the biomass is concentrated by dewatering to more than 10% dry matter content. Before the hydrothermal carbonization, the biomass is brought to a pH of less than 4. The process waste heat produced by the hydrothermal carbonization is used for subsequent drying of the resulting product.

German Offenlegungsschrift DE 10 2008 028 953 A1 discloses a process for the production of coal from plants and plant residues. For this purpose, the raw biomass (wood, plant parts, eg straw, plant residues) is comminuted. It wants to achieve a particle size of 5 to 50 mm. The mostly still moist biomass is immersed in a water bath and filled in a pressure-resistant reaction vessel. The container contents are from ambient to the desired reaction temperature, eg. B. 180 ° C, heated. Likewise, the tank pressure is raised to a level above the value corresponding to the evaporation pressure at the set process temperature. During the reaction process, the reaction process enters an exothermic phase where part of the energy chemically bound in biomass is converted to heat. After the carbonation process has ended (eg 8 to 12 hours, depending on the biomass used and the pressure or reaction temperature), the container is cooled down to the point where a safe pressure reduction to ambient pressure level is possible. The container is then opened and emptied. The coal is filtered from the process water, mechanically dewatered and treated. The reaction vessel is operated intermittently.

The German patent application DE 10 2008 058 444 A1 describes a method and an apparatus for the production of fuels or fuels. The raw materials or fuels are produced from a solid / liquid mixture of water and a carbon-containing component. The solid / liquid mixture is at a temperature of about 100 ° C and a pressure handled by over 5bar. In this case, starting materials are fed via a heat exchanger continuously to a first reactor and the reaction mixture is passed in batches from one to the next reactor and continuously removed reaction products from the last reactor. The reaction space serves to receive a solid / liquid mixture, for example biomass. The reactor has a brewing device with which the solid / liquid mixture can be mixed during treatment and / or processing.

International patent application WO 2008/081407 A2 discloses a plant and / or fuel produced from biomass. The biomass is treated in at least one reactor for receiving solid / liquid mixtures. After the treatment of the biomass obtained from the biomass, the desired plant and / or fuel.

European Patent Application EP 1 970 431 A1 also discloses a method and apparatus for the hydrothermal carbonization of biomass. In this case, the starting materials are introduced through an inlet into a pressure reactor during an ongoing carbonization process. With a conveyor, the reaction products within the reactor are moved from the inlet to the outlet. At the outlet then the biomass converted to a large extent to end products can be removed.

International Patent Application WO 2008 / 095589A1 discloses the hydrothermal carbonization of biomass. It is proposed that biomass, water and / or at least one catalyst can be supplied to a pressure vessel designed substantially as a pipeline with at least one controllable inlet opening and at least one controllable outlet opening via the at least one controllable inlet opening. The temperature and / or pressure conditions are controlled in the pressure vessel such that the product supplied to the pressure vessel contents of biomass, water and catalyst transported in the pipeline is, with biomass, water and catalyst react with each other and at least one reaction product of the contents is removed via the at least one controllable outlet opening.

International Patent Application WO 2008/193309 discloses a method for converting biomass into higher energy density solids, especially coal, humus or peat. In the process, organic substances from the biomass are slurried to form a suspension in water, and a part of the suspension to be converted is heated to a reaction temperature and converted at elevated pressure by hydrothermal carbonation into the higher energy density solids. The method is characterized in that the conversion is carried out in a reaction volume that is below the surface of the earth.

European Patent Application EP 2 130 893 A2 discloses a method for producing coal, in particular coal sludge. The coal slurry is made from moist biomass, in particular sewage sludge by hydrothermal carbonization, wherein the carbon structure of the biomass is preferably broken at at least 180 ° C to 200 ° C with exclusion of air. The process proceeds in particular in batch mode, wherein the biomass is concentrated by dehydration to values above 10% dry matter content before the hydrothermal carbonization. Before the hydrothermal carbonization, the biomass is brought to a pH <4. The process waste heat generated during the hydrothermal carbonization is used for the subsequent drying of the resulting product. Dosing devices, pumps and valves are used to feed parallel reactors. The reactors have a stirrer to improve the reaction. Alternatively, tubular reactors can be used which ensure a good mixing of the sewage sludge. In contrast to fossil fuels, biomass comprises renewable raw materials, which are available as domestic energy sources in the long term, as well as all liquid and solid organic substances and products of biological and biochemical processes and their transformation products, which have a sufficiently high carbon content for this process and otherwise in their Composition and nature of economically useful reaction, intermediate, by-products and end products can be processed by the hydrothermal carbonization to fuels. For example, the starting materials include carbohydrates, sugars and starches, agricultural and forestry products, as well as specially grown energy crops (fast-growing tree species, reed grasses, cereal crops, etc.), soybeans, sugarcane and cereal straw, as well as biogenic residues, wastes and by-products. Plants and plant remains of other origin

(Roadside greenery, landscaped property, etc.), agricultural waste including straw, sugar cane leaves, sprouting cereals, unsaleable lots of potatoes or sugar beet, spoiled silage, as well as other leftovers, grass clippings, cereal straw, beet leaves, sugar cane leaves, carbonaceous residues and waste, including organic waste, high-calorific fractions of domestic and commercial waste (residual waste), sewage sludge, various types of wood and classes, including forest wood, timber,

Pallets, used furniture, sawdust, leftovers and waste from the food industry, including catering waste, garbage, waste oils, paper and cellulose, textiles, in particular of natural fibers and natural

Polymeric and animal excrements, including manure, horse manure and poultry droppings.

From DE 197 23 510 C1, for example, a device for the treatment of biogenic residual masses is known which comprises a cylindrical reactor, in the food waste u. Ä. Be subjected to a temperature-pressure hydrolysis. The reactor is designed as a loop reactor with a heatable jacket surface. By means of a pump, a flow is generated within the reactor, which ensures thorough mixing of the suspension. The invention has for its object to provide a plant for the production of carbonaceous products from biomass by hydrothermal carbonation, which ensures a substantially continuous operation of the plant, so that a continuous supply of biomass is possible in the system and that also a continuous decrease of end products from the plant is possible.

The object is achieved by a system comprising the features of claim 1.

Another object of the invention is to provide a method by which products from the hydrothermal carbonization of biomass can be generated essentially by means of a continuous operation.

This object is achieved by a method comprising the features of claim 12.

The plant for the production of carbonaceous products from biomass by means of the hydrothermal carbonization comprises a first area 100, in which the provision, reduction and mixing of different types of biomass is performed. As mentioned above in the description of the prior art, in the hydrothermal carbonization according to the present invention, possible biomass containing some carbon can be processed. In a second area of the plant, the processing and preparation of the mixed biomass takes place. In the second area of the biomass process water and a catalyst is added to adjust the required for the subsequent reaction process proportion of the dry matter in the reaction mixture. The second area is followed by a third area in which the reaction process according to the hydrothermal carbonization is carried out. The third area is followed by a fourth area, which serves to further process the reaction products. The third area consists of at least three reactors. The at least three reactors are interconnected via a first line system, a second line system and a third line system. The first conduit system is guided via a first heat exchanger, so that at least one of the at least three reactors can be controlled and selectively filled with biomass from the second region. The second line system is also passed through a heat exchanger. Furthermore, a pump is provided in the second line system so that biomass in the reaction process can be controlled from the active reactor of the at least three reactors and selectively circulated during the reaction process. At least one stirrer is provided in the reactor, which additionally serves for thorough mixing and circulation of the biomass. The pump thus achieves good mixing of the reaction products in the active reactor of the at least three reactors. A third line system is led from the at least three reactors via a heat exchanger. About the third line system, the reaction products of the completed reaction process are withdrawn from the active reactor and fed via a relaxation device the fourth area. The reaction products are only withdrawn from the active reactor when the reaction process in the active reactor has come to a standstill.

The at least three reactors of the third region are operable in such a way that at least one reactor is the active reactor. At least one other reactor is the reactor that is being filled with the added biomass from the second area. At least one further reactor is the reactor being emptied. This reactor was the previous active reactor in which the reaction process has come to an end, so that its content can be transferred to the fourth region for further processing of the reaction products. For control in the third area, the first line system, the second line system and the third line system are provided with a plurality of controllable two-way valves and a plurality of controllable three-way valves. The entire hydrothermal carbonization plant is connected to a program control so that the specific filling, circulation and discharge of the at least three reactors in the third area can be regulated or controlled.

The first area for the provision, crushing and mixing of at least one type of biomass comprises a multitude of acceptance and storage positions for the unmixed provision of the different types of biomass. In the first area, at least one comminution unit and a mixer for the different biomasses are provided. The comminution unit is necessary in order to produce the biomass to a required particle size or a range of the process-usable particle sizes of the biomass.

The second area has a mixing tank in which the comminuted and mixed biomass is filled. In the mixing vessel, the comminuted and mixed biomass is further added via a line with process water. Via a third line, which opens in the second line for the process water, a catalyst required for the reaction process of the hydrothermal carbonization can be added to the process water. The process water and the catalyst are fed together via a mixer. An agitator operated by a motor is provided in the mixing vessel in order to ensure good mixing of the biomass with the process water and the catalyst. In addition, it is avoided by means of the agitator settling of the biomass at the bottom of the mixing vessel. By the added amount of process water to the mixed and comminuted biomass can thus adjust the proportion of dry matter in the reaction process, which takes place downstream in at least one of the reactors. In the mixing container If you set a dry matter content of 20% to 60%. The proportion of the dry substance depends essentially on the fraction of the various types present in the comminuted and mixed biomass and the resulting reaction processes in the downstream reactors.

From the second area, the biomass mixed with process water and catalyst reaches the third area via a third line, in which the reaction process is carried out. In the line, a pump is provided so as to be able to adjust the filling rate of the at least one reactor in the third range. In the fourth region, a collecting vessel for receiving the reaction products from the at least one reactor is provided for further processing of the reaction products, from which the reaction products are removed. The reaction products are only then removed from the initially active reactor, after which the reaction process is completed in this reactor. The collecting container also has a motor operated agitator. Via a pumped line, the reaction products are fed to a dehydrator and a downstream dryer.

From the dewatering device, a line leads to a collecting container for the process water obtained in the dewatering device. The process water is returned to the second area via a line provided with a pump. Thus, the process water can in turn be introduced into the reaction cycle. The process water is thus fed to the mixed and comminuted biomass in the mixing container provided in the second area. The reaction product is removed from the dryer after the drying process and fed to a collecting container. From the collection of packaging or removal can be organized. According to a further embodiment of the invention, a fifth region may be provided. The fifth area can be at least part of the Reaction products are fed directly from the at least one active reactor. The reaction products are, as already mentioned above, only taken from the at least one active reactor, if in this the reaction process has been completely completed. These reaction products, which are supplied to the fifth region, have a dry matter content of about 10%. In the fifth zone, carbon dioxide is added to the reaction products. The carbon dioxide comes z. B. from the coal combustion of a fossil power plant. Any combustion process that produces carbon dioxide can be used as a carbon dioxide source. Carbon dioxide can thus be supplied to the fifth region of the plant and is thus involved in the production of synthesis gas.

The plant is in the first area, in the second area, in the third area, in the fourth area and in the fifth area a variety of controllable two-way valves and three-way valves, thereby controlling a material flow within the plant via a central program control, or can be adjusted.

The plant can be used to produce coal and / or synthesis gas as a reaction product. It is possible by appropriate program control to adjust the reaction product to the needs of a customer so that the fuel is an optimal performance during combustion. The setting and additional elements of the coal contained in the fuel can be adjusted to the reaction process by suitable selection of the starting products of the various biomass types.

The process for the production of carbonaceous products from biomass by means of the reaction process of the hydrothermal carbonization is characterized by the following steps: First, the biomass of different types is provided in a first region. For the provision of the biomass, various containers, silos or Storage spaces are provided. In these storage areas or silos, the biomass is stored separately by type. In the first area, the biomass is now taken from the different storage locations according to the desired composition for the reaction process. The biomass is fed to a crushing and mixing, and ultimately transferred to a second area of the plant. In the second area, the mixed and comminuted biomass is mixed with process water and a catalyst, so that a required for the reaction process content of biomass dry matter is adjusted. In a third area at least three reactors are provided. In order to produce a continuous process for the production of fuel or carbon-containing reaction products, the process is designed such that at least one reactor of the reactors provided in the third region is filled with the biomass, which is mixed with process water and catalyst. In at least one further reactor, which is referred to as an active reactor, is just starting the reaction process in which the biomass is converted into a carbon-containing reaction product. Parallel to the filling of the at least one reactor and to the currently active reactor in which the reaction process takes place, at least one further reactor is emptied. This reactor, which is being emptied, is the reactor that was previously the active reactor and in which the reaction process is complete. The reaction products which are taken from the at least one reactor are fed to a fourth region. In the fourth area, dehydration and drying of the reaction products withdrawn from the at least one reactor of the third area occur.

The reaction products taken from the reactor of the third range have a dry matter content of about 10%. In the downstream dewatering in the fourth range, a dry matter content of about 50% is set. For further drying The reaction products ultimately a dry matter content of about 90% is achieved.

In order to achieve a well-proceeding reaction process in the at least one reactor of the third range, the biomass is constantly circulated via a heat exchanger. After completion of the reaction process in the at least one active reactor, the biomass is discharged from the reactor and thereby fed via a third heat exchanger and a relaxation device the fourth area.

As already mentioned above, a fifth region can also be provided in the system in which at least part of the reaction products can be supplied from the active reactor after completion of the reaction process. It is also possible that all of the reaction products withdrawn from the active reactor are fed to the fifth region. Synthesis gas is generated in the fifth area. A program control controls the material flow within the system for carrying out the method.

With the method according to the invention, a fuel can be produced, which is carbonaceous. The fuel can be a coal. According to another embodiment of the invention, the fuel may be synthesis gas.

In the following, embodiments of the invention and their advantages with reference to the accompanying figures will be explained in more detail.

FIG. 1 shows a schematic representation of the invention

Plant for carrying out hydrothermal carbonation. Figure 2 shows a schematic representation of another

Embodiment for carrying out the reaction process of the hydrothermal carbonization. FIG. 3 shows a further embodiment of the plant for carrying out the reaction process of the hydrothermal carbonization.

FIG. 4 shows a schematic representation of the first region of FIG

Plant for hydrothermal carbonization, in which the different biomass required for the reaction process can be comminuted and mixed.

FIG. 5 shows a schematic representation of the second region of FIG

Hydrothermal carbonation plant in which the comminuted and mixed biomass are mixed with process water and catalyst before they are sent to the reaction process.

Figure 6 shows a schematic representation of the third area, in which at least three reactors are provided, which are connected to each other via different lines.

Figure 7 shows a schematic representation of the elements of the fourth

Area of the hydrothermal carbonation plant, where finally the reaction products are processed for further consumption.

FIG. 8 shows a schematic representation of a reactor in FIG

Connection with an associated heat exchanger.

For identical or equivalent elements of the invention, identical reference numerals are used. Furthermore, for the sake of clarity, only reference symbols are shown in the individual figures, which are required for the description of the respective figure or for the arrangement of the figure in the context of other figures.

Figure 1 shows the schematic structure of the plant 1 for hydrothermal carbonization. In the embodiment shown in Figure 1, the plant is 1 for hydrothermal carbonization of a first region 100, a second region 200, a third region 300 and a fourth region 400 formed. The first area 100, the second area 200, the third area 300 and the fourth area 400 are connected by means of a common program control 10. In the first area 100, the assembly and mixing of the different biomasses takes place. From the first region 100, the thus mixed and comminuted biomasses reach the second region 200, in which a processing and preparation of the mixed biomasses is carried out. Process water PW is added to the crushed and mixed biomasses. From the second region 200, the biomass mixed with process water PW reaches the reactor region, which is referred to as the third region. In the third area, the reaction process of hydrothermal carbonation takes place. After the reaction process is completed, the finished reaction product is supplied to the fourth area where processing of the reaction products of the hydrothermal carbonization process is performed. In the fourth area, process water PW is recovered, which is ultimately returned to the second area for reuse.

FIG. 2 shows a further embodiment of the plant 1 for the hydrothermal carbonization of biomass. Here, the fourth area is exchanged for a fifth area 500. The reaction products from the third region, which are taken from the reactor which was previously the active reactor and in which now the reaction process is completely completed, are fed directly to this fifth region. These reaction products have a dry matter content of about 10%. In the fifth region 500, a reaction process is performed in which synthesis gas is generated. For the production of the synthesis gas carbon dioxide C0 _{2 is} supplied in the fifth area. The supplied carbon dioxide may, for. B. originate from a carbon dioxide source 15. A carbon dioxide source 15 is z. B. a fossil power value, o. Ä. Thus, directly from the fossil power plant formed and formed carbon dioxide to the process for Synthesis gas extraction in the fifth region 500 of Appendix 1 are supplied.

FIG. 3 shows a further embodiment of the invention. Here, in addition to the fourth area 400, the fifth area 500 is provided. A part of the finished reaction products is thus supplied from the third region to the fourth region 400. In the fourth area, the dewatering and drying of the reaction products already mentioned in the description of FIG. 1 thus takes place. The thus obtained process water is supplied from the fourth area 400 again to the second area 200. Another portion of the reaction products from the third region 300 may be supplied to the fifth region 500 where synthesis gas is ultimately generated with the addition of carbon dioxide from a carbon dioxide source 15.

Analogous to the description of FIG. 1, the embodiments of the systems mentioned in FIGS. 2 and 3 are also assigned a program control 10 by means of which the material flow in the most varied embodiments of the system 1 can be controlled and regulated.

FIG. 4 shows a schematic representation of the first region 100 of the plant 1 for the hydrothermal carbonization of biomass. The first area comprises a plurality of acceptance and storage locations 12 _; 12 ₂ , 12 _n for the different types of biomass 5 _; 5 ₂ , 5 _n . The embodiment of the region 100 shown in FIG. 4 represents only one possible form of embodiment and should not be construed as a limitation. It is obvious to a person skilled in the art that the first area 100 can be designed according to the customer's requirement. The number of acceptance and storage locations 12 _; 12 ₂ , 12 _n , depends on the different types of biomass that are to be processed in Appendix 1. Likewise, the number of comminution units 13 depends on the type of biomass that is to be processed with the system 1. After the appropriate comminution of the biomass these become a mixer 14 supplied, in which the mixed biomass 5N is provided for the further reaction process.

In the embodiment of the first region 100 shown in FIG. 4, a first comminution unit 13 and a second comminution unit 13 _{2 are} provided. The first crushing unit 13i is designed as a crusher. The second crushing unit 13 ₂ is designed as a hammer mill. The first crushing unit 13 are thus supplied large pieces of biomass, which still require a strong crushing before they are fed to the mixer. The second crushing unit 13 ₂ is designed as a hammer mill and thus can already shredded parts of biomass, such. B. Strohabfälle, grass clippings, bark waste, wood chips, etc. continue to shred and feed them directly to the mixer 14. Likewise, in the embodiment of Figure 4 an acceptance and storage point 12 ₃ for already liquid biomass is present. This liquid biomass can z. B. sewage sludge. The biomass comminuted with the first comminuting unit 13 is thus supplied to a feed line of the liquid biomass from the receiving and storing point 12 ₃ . Thus, the biomass coming from the first crushing unit 13i is already mixed with a liquid biomass before it reaches the mixer 14. From the mixer 14, the biomass passes via a line 1 1 1 in the second area 200. The second area 200 of the system 1 comprises a mixing container 21st In the mixing vessel 21, a stirrer 220 driven by a motor 221 is provided. In the mixing vessel 21 passes through the line 1 1 1, the mixed biomass 5N. In parallel, the process water PW is supplied to the mixing vessel 21 via a line 21 1. In line 21 1 for the process water PW, a mixer 214 is inserted. Before the process water PW passes via the line 21 1 in the mixer, opens into the line 21 1, a line 212 which feeds a catalyst from a tank 213 in the process water. The catalyst may, for. For example, formic acid, citric acid or sulfuric acid. After the mixed biomass 5N and the process water PW are sufficiently mixed in the mixing vessel 21, the so achieved mixture, which has a dry matter content of 20% to 60%, via a line 222, which is provided with a pump 30, the third region 300 is supplied.

In the lines shown in Figure 5, a plurality of two-way valves 32 is provided. These two-way valves 32 are connected to the program controller 10. Thus, it is possible to selectively control the material flow through targeted control of the two-way valves and thus z. B. to set the dry matter content in the mixing container 21 targeted. The size of the dry matter content depends essentially on the downstream process conditions in the third range.

The structure of the third region 300 is shown schematically in FIG. The third region 300 comprises at least three reactors 301. Each of the reactors is provided with a positive pressure line 302 which terminates in a controllable two-way valve 32. By means of this controllable two-way valve 32, the pressure inside the reactor can thus be adjusted to a predefined level. It is also possible to release the pressure if, in the interior of the at least one reactor 301, the pressure rises above a predefined level. In the third area 300 of Appendix 1, at least three reactors 301 must be present to ensure continuous production of the reaction products of the hydrothermal carbonation process. At least one reactor 301 of the reactors is an active reactor 301 A. The term "active reactor" means that in this reactor 301, the process of hydrothermal carbonization takes place and is not yet completed.

In at least one other reactor 301 of the at least three reactors biomass is introduced via a line 31 1 in the reactor 301. This reactor 301 is referred to as fillable reactor 301 F. In the in Figure 6 shown schematic representation of the third area 300 of Appendix 1, two fillable reactors 301 F are provided. The fillable reactors 301 F are filled via line 31 1 with the mixed with process water and catalyst biomass. In line 31 1, a first heat exchanger 310 is introduced. Furthermore, the line 31 1 connects all the reactors 301 of the third area 300. Via a controllable three-way valve 33, the line 31 1 can thus be disconnected in the direction of the at least one fillable reactor 300F so that the reactor 301F can be provided with biomass, process water and Catalyst can be filled. Furthermore, a second line system 321 is provided, which likewise connects each reactor 301 of the third area 300 to one another. The second line 321 is designed as a ring line and is also guided via a second heat exchanger 320. Furthermore, a pump 30 is provided in the line 321, with which the biomass from the at least one active reactor 301 A is constantly pumped through the second heat exchanger 320. By this pumping one reaches a constant mixing of the biomass in the active reactor 301 A. In the interior of each reactor 301, at least one stirrer 350 is provided, which additionally serves for thorough mixing and circulation of the biomass 5-i, 5 ₂ , 5 _n . The stirrer 350 is preferably arranged in the lower region of the reactor 301. In the designed as a ring line second line 321 a plurality of three-way valves 33 and two-way valves 32 are provided so as to circulate the material flow of just reacting in the active reactor 301 A biomass via the loop 321 and the heat exchanger. The two-way valves 32 and the three-way valves 33 are controlled such that the second line 321 with the at least one active reactor 301 A forms an open ring, so that the pumping of the biomass during the reaction process in the active reactor 301 A is possible.

At least one further reactor 301 of the reactors in the third region 300 is a reactor 301L which is about to be emptied previously the active reactor 301 A. after the reaction process in the active reactor 301 A is completed, the reaction products can be removed from the reactor. The active reactor 301 A then becomes the empty reactor 301 L. Each of the reactors 301 is connected to a third line 321, which is passed through a third heat exchanger 320. In the third conduit 331, a plurality of two-way valves 32 and three-way valves 33 are also provided, thus controlled to connect the empty reactor 301 L to the third conduit 331. The reaction product withdrawn from the emptying reactor 301 L is passed via the third line 331 via an expansion device 340, so that the reaction products are brought substantially to an ambient pressure level. From the expansion device 340, the reaction products reach the fourth region 400 and / or the fifth region 500, in which, as already mentioned, synthesis gas can be produced. For the further description of the invention, the fifth region 500 is omitted, in which synthesis gas can be prepared from the reaction products in conjunction with carbon dioxide. In the description of the present invention, as shown in Figure 7, the reaction product now passes via the line 331 in the fourth area and is spent there in a collecting container 41. In the collecting container 41, a stirrer 420, which is driven by a motor 421, is arranged. Via a line 41 1, in which a pump and at least one controllable two-way valve 32 are provided, the reaction product is placed in a dewatering device. The reaction products fed in via line 331 have a dry matter content of about 10%. In the dehydrator 430, the dry matter content is increased to about 50%. The process water PW obtained from the reaction products passes into a collecting container 436. Should the level in the collecting container 436 become too high, the excess process water PW is discharged via an overflow 437 to the environment. About the line 31 1, which is provided with a pump 30 and a two-way valve 32, the Process water PW returned to the second area 200 of Appendix 1. From the dehydrator 430, the reaction product passes into a dryer 432. The dryer is driven by a motor 433. In the dryer 432, the dry matter content of the reaction products is increased to about 90%. From the dryer 432, the dried reaction product passes into a collecting container 434. From the collecting container 434, the distribution to the consumers of the reaction products prepared with the plant 1 can finally take place.

FIG. 8 shows a simplified schematic representation of the active reactor 301 A in conjunction with the ring line 321 and the second heat exchanger 320. During the reaction process taking place in the active reactor 301 A, the biomass which is currently reacting is constantly transferred via the pump 30 and the ring line 321 second heat exchanger 320 recirculated. Thus, one achieves a constant circulation of reacting in the active reactor 301 A biomass. In order to initiate the reaction process in the active reactor 301 A, the filled biomass is brought to a certain temperature and a certain pressure. During the pumping of the just reacting biomass via the line 321, the temperature and the pressure prevailing in the active reactor 301 A pressure is maintained substantially. By pumping the currently reacting biomass to save mechanical components that need to be introduced with a passage in the active reactor 301 A and the other reactors 301. By pumping the reacting biomass in the active reactor 301 A thus possible leakage through the implementation in the active reactor 301 A is avoided. This results in a much higher production reliability with the system 1 according to the invention.

In the embodiment shown in FIG. 6, four reactors 301 are shown. These reactors 301 may take on different functions depending on the end of the production process. Thus, at least one reactor 301 may be the active reactor 301 A. Is the If the at least one reactor 301 a that can be emptied is completely emptied, the reactor 301 becomes the fillable reactor 301 F. How many reactors 301 are active reactors 301 A or emptying reactors 301 L or refillable reactors are 301 F depending on the process conditions to ensure a continuous output of reaction products.

The invention has been described with reference to preferred embodiments. It will be understood by those skilled in the art that changes and modifications may be made without departing from the scope of the following claims.

Claims

claims

Plant (1) for the production of carbonaceous products from biomass (5-i, 5 ₂ , 5 _n ) by means of hydrothermal carbonation, with a first region (100) for providing, comminuting and mixing at least one tee of biomass (5-i, 5 ₂ , 5 _n ), a second area (200) for preparing and preparing the mixed biomass (5M), a third area (300) for carrying out a reaction process according to hydrothermal carbonation and at least a fourth area (400) for further processing of the reaction products of Reaction process, characterized in that the third region (300) comprises at least three reactors (301) that a first conduit system (31 1) over at least one first heat exchanger (310) is guided, so that at least one reactor (301) of at least three Reactors (301) is a reactor which can be filled (301 F) and is controlled and selectively filled with mixed biomass (5M) from the second zone (200) a second conduit system (321), in which a pump (30) is inserted, is guided over at least one second heat exchanger (320), so that in

Reaction process located biomass from one of the at least one active reactor (301 A) of at least three reactors (301) controlled and selectively circulated; by means of which the reaction products in the active reactor (301 A) can be pumped during the reaction process and wherein in the reactor (301) at least one stirrer (350) is provided which additionally for a

Mixing and circulation of the biomass (5-i, 5 ₂ , 5 _n ) serves that a third line system (331), starting from the at least three reactors (301) via at least one third heat exchanger (330) is guided over the after a completed Reaction process the reaction products from a reactor which can be emptied (301 L), in which the reaction process of the hydrothermal carbonization is completed, of at least three

Reactors (301) removable and via a relaxation device (340) the fourth region (400) can be fed.

2. Installation according to claim 1, wherein the first conduit system (31 1), the second conduit system (321) and the third conduit system (331) with a plurality of controllable two-way valves (32) and a plurality of controllable three-way - Valves (33) are provided, which are connected to a program control (10) of the system (1), so that the specific filling, circulation and emptying of the at least three reactors (301) is controllable.

3. Plant according to claims 1 to 2 wherein the first region (100) for

Provision, comminution and mixing of at least one type of biomass (5-I, 5 ₂ , 5 _n ) a plurality of acceptance and storage sites (12 _; 12 ₂ , ... 12 _n ) for the unmixed provision of the different types of biomass (5 -i, 5 ₂ , 5 _n ), at least one comminuting unit (13) and a mixer (14) for the different biomasses (5-i, 5 ₂ , 5 _n ).

4. Plant according to claims 1 to 2 wherein the second region (200) a

Mixing container (21), in which a first line (1 1 1) with mixed biomass (5M) from the first region (100) and a second line (21 1) for process water (PW) into which a third line (212 ), wherein the process water (PW) and the catalyst by means of a mixer (214) are miscible and wherein in the mixing vessel (21) with a motor (221) operated agitator (220 ) is arranged.

Plant (1) according to claim 4, wherein a third conduit (222) is provided with a pump (30), by means of which the process water and catalyst and mixed biomass (5M) is supplied to the third area (300) for carrying out the reaction process can be fed.

6. Plant (1) according to claims 1 to 2 wherein the fourth region (400) for

further processing of the reaction products comprises a collecting container (41) for receiving the reaction products from the at least one active reactor (301 A), in which the reaction process is completed, wherein the collecting container (41) with a motor (421) operated agitator (420) has, that via a first provided with a pump (30) line (41 1) with a dewatering device (430) and a downstream dryer (432) is connected.

7. Plant according to claim 6, wherein a second line (421) the

Dewatering device (430) with a collecting container (436) for

Process water (PW), wherein the process water (PW) via the pump (30) provided with line (21 1) the second region (200) can be supplied and wherein the reaction product from the dryer (432) a collecting container (434) for the removal can be fed.

8. Plant according to claims 1 to 7, wherein a fifth region (500) is provided, which at least a portion of the reaction products from the at least one active reactor (301 A) can be fed and in the fifth region (500) in a

Synthesis gas is convertible.

9. Plant according to claim 8, wherein the fifth region (500) for producing the

Synthesis gas is connected to a carbon dioxide source (15).

10. Plant according to one of claims 1 to 9, wherein in the first region (100), in

second area (200), in the third area (300), in the fourth area (400) and in the fifth area (500) a plurality of controllable two-way valves (32) and three-way valves (33) are provided , whereby a material flow within the system via a program control (10) is adjustable.

1 1. Use of the plant according to claims 1 to 10, for the production of

Coal (K) and / or synthesis gas (SG) as reaction product.

12. Process for the production of carbonaceous products from biomass

by the reaction process of hydrothermal carbonation

characterized by the following steps:

• that biomass (5-i, 5 ₂ , 5 _n ) of different types in a first

Area (100) is provided;

That the biomass (5M) comminuted and mixed in the first region (100) from different types of the biomass (5-i, 5 ₂ , 5 _n ) in a second region (200) is mixed with process water (PW) and a catalyst, so that a required for the reaction process content of biomass dry matter is set, • that in a third area (300) at least three reactors (301) are provided, wherein at least one reactor (301 F) with the process water (PW) and catalyst offset biomass from the second region (200) via a first heat exchanger (310 ) is filled, that at least one reactor (301) is an active reactor (301 A), in which the biomass is converted into reaction products during the reaction process and that at least one reactor (301 L) is emptied, in which the reaction process is completed;

That during the reaction process in the at least one active reactor (301 A), the biomass via a second heat exchanger (320) with a pump (30) is circulated and wherein in the reactor (301) at least one stirrer (350) is provided by the in addition, mixing and circulation of the biomass (5-i, 5 ₂ , 5 _n ) is carried out; and

A fourth area (400) after completion of the reaction process, the reaction products from the at least one reactor (301 L) of the third area (300), which is emptied, via a third heat exchanger (330) and a relaxation device (340) in the fourth area (400) to a dewatering device (430) and a dryer (432) are supplied.

13. The method of claim 12, wherein a fifth region (500) is provided in which at least a portion of the reaction products from the at least one active reactor (301 A) is supplied after completion of the reaction process, wherein the reaction products in the fifth region (500). be converted into a synthesis gas (SG).

14. The method according to any one of claims 12 to 13, wherein a program control (10) is provided by the in the first region (100), in the second region (200), in the third region (300), in the fourth region (400) and in the fifth area (500) a plurality of two-way valves (32), three-way valves (33) and pumps (30) is controlled, whereby a material flow within the system (1) via the program control (10) regulated becomes.

15. A carbonaceous reaction product prepared according to the process of claims 12 to 14.

16. A carbonaceous reaction product according to claim 15, wherein the

carbonaceous reaction product is coal (K).

The carbonaceous reaction product of claim 15, wherein said

carbonaceous reaction product is synthesis gas (SG).