DE102010000580A1 - A system and method for providing a mixture of different biomass to a plant for recovering a reaction product from the different biomass - Google Patents

Abstract

A system (100) and a method for providing a mixture of different types of biomass (51, 52, ..., 5n) for a plant (1) for hydrothermal carbonization are disclosed. With a large number of reception and storage points (121, 122, ..., 12n) for the different types of biomass (51, 52, ..., 5n), at least one shredding unit (13) and at least one mixer (14) for creating a homogeneous mixture of at least two of the different types of biomass (51, 52, ..., 5n) provided. Each acceptance and storage point (121, 122, ..., 12n) is assigned an analysis unit (151, 152, ..., 15n), by means of which a content in the different types of biomass (51, 52, ..., 5n) of foreign and / or pollutants can be determined.

Description

The present invention relates to a system for providing a mixture of different types of biomass for a plant for producing a reaction product by means of a reaction process.

The system for providing a mixture of different types of biomass to a plant for producing a reaction product by means of a reaction process comprises a plurality of acceptance and storage sites for the different types of biomass. Likewise, at least one shredding unit and a mixer are provided to produce a substantially homogeneous mixture of at least two of the different types of biomass for further processing.

The plant is used to produce carbonaceous products from biomass using hydrothermal carbonation. Furthermore, the system according to the invention can also be used in a plant for the production of biogas.

Furthermore, the invention relates to a method for providing a mixture of different types of biomass for a plant for producing a reaction product by means of a reaction process.

The plant may according to a preferred embodiment for the production of carbonaceous products from biomass comprises a first region in which the system according to the invention is contained. The system provides, comminutes and mixes at least one type of biomass. 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.

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 carried out E. Behrl et al. Chem. 493 (1932), pp. 97-123 ; Angew. Chemistry 45 (1932), pp. 517-519) and through 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 are the publications of Wang et al., Carbon 39 (2001), pp. 2211-2214 and the publication of X. San and Y. Li, Angew. Chem. Int. Ed. 43 (2004), pp. 597-601 ) to mention.

The international patent application WO 20 10 006 881 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.

The German patent application DE 10 2008 007 791 A1 discloses an apparatus for aqueous charring of biomass and carbonization products obtained thereby. Biomass can be converted to coal by the process of hydrothermal carbonation. Disadvantages of previous methods consist in the high energy consumption for the process cooling and the process start. By this device, the efficiency is increased, simplifies the process flow and process reliability can be improved. By using a boiling point suitable coolant energy-saving, automatically dosing, reliable discharge of the process heat is realized as a result of directed Siedekreislauf. A tilt mechanism replaces an agitator and ensures thorough mixing and uniform heat distribution in the process vessel. By storing the process heat of the exothermic process and the use for follow-up processes, external heating is avoided.

The German patent application DE 10 2008 028 953 A1 discloses a process for producing 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, he warms. Likewise, the tank pressure is raised to a level above the value corresponding to the evaporation pressure at the set process temperature corresponds. 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 international patent application WO 2008/120662 A1 discloses a continuous reactor for the treatment of biomass. The hydrothermal reaction proceeds in a high pressure reactor. The reactor is assigned a supply of starting material. The continuous hydrothermal reaction device is a high pressure reaction device. There is provided a material supply unit comprising a biomass kneader and pumps so as to transfer the slurry into a tube reactor. The tube reactor is made of corrosion-resistant metal. Further, an isothermal heater and water cooling is provided. The material from the reactor via electromagnetic valves. Furthermore, the reactor comprises a pressure buffer, wherein the biomass in the tube reactor is exposed exclusively to controlled high-pressure hydrothermal reaction conditions.

The German patent application DE 10 2008 058 44 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 treated at a temperature of over 100 ° C and a pressure of about 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.

The international patent application WO 2008/081407 A2 discloses a biomass-produced plant and / or fuel. 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.

The European patent application EP 1 970 431 A1 also discloses a method and apparatus for 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.

The international patent application WO 2008 / 059989A1 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 so that the product supplied to the pressure vessel biomass, water and catalyst is transported in the pipeline, wherein biomass, water and catalyst react with each other and the at least one controllable outlet at least one reaction product of the Contents is taken.

The international patent application WO 2008/193309 discloses a method for converting biomass to 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.

The European patent application EP 2 130 893 A2 discloses a process 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, whereby the biomass is reduced to more than 10% by dewatering before the hydrothermal carbonization. Dry matter content is concentrated. 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.

The European patent application EP 1 762 607 a biogas plant control method for a biogas plant, which consists of a fermenter tank and at least one metering device for a basic biomass. The control device is used to control at least one process parameter as a controlled variable of the fermentation process.

The German Utility Model DE 201 06 837 U1 discloses a fermenter tank with a conveyor, by means of the recorded in a mixing and storage organic solids as a substrate mix batchwise in the fermenter container can be introduced. The conveyor is a screw conveyor, so that a well-defined substrate mix enters the fermenter tank in batches.

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. Plant and plant remains of other origin (roadside greenery, landscape care goods, etc.), agricultural waste including straw, sugar cane leaves, Abputzgetreide, unsellable batches of potatoes or sugar beet, spoiled silage, and other leftovers, grass clippings, cereal straw, beet leaves, sugar cane leaves, carbonaceous residual and Waste materials, including biowaste, high-calorific fractions of domestic and commercial waste, sewage sludge, various types of wood and classes, including forest wood, lumber, pallets, used furniture, sawdust, food industry waste and waste, incl Lich catering waste, waste vegetables, waste grease, and pulp and paper, textiles, in particular of natural fibers and natural Polymären and animal waste, including manure, horse manure and poultry droppings.

From the DE 197 23 510 C1 For example, a device for treating biogenic residual masses is known which comprises a cylindrical reactor in which food waste u. Ä. Be subjected to a temperature-pressure hydrolysis. The reactor is designed as a loop reactor with a heated 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 system for providing a mixture of different types of biomass, with which a foreign and / or pollutant content is adjustable in the reaction product to provide.

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 a foreign and / or pollutant content in the reaction product can be adjusted.

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

In the system according to the invention, according to one embodiment, the reaction process for the production of biogas can be configured. According to another embodiment, the reaction process is the hydrothermal carbonization of biomass. A program control is used to detect the values of the at least one analysis system, by means of which the content of foreign and / or pollutants in the different types of biomass can be determined. The process parameters of the reaction process and the system are then controlled so that the content of foreign and / or pollutants in the reaction product is defined adjustable.

According to a possible embodiment, the plant as a plant for the production of carbonaceous products from biomass by means of the hydrothermal carbonization comprises a first region formed by the system according to the invention, in which the provision, comminution and mixing of the different types of biomass is carried out. As mentioned above in the description of the prior art, can at the hydrothermal carbonization according to the present invention possible biomass are processed, which contains a certain amount of carbon. 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 at least one 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 system for providing a mixture of different types of biomass for a hydrothermal carbonation plant includes a multitude of acceptance and storage sites for the different types of biomass. At least one shredding unit and mixer are provided for creating a homogeneous mixture of at least two of the different types of biomass. Each acceptance and storage point is an analysis system can be assigned, by means of which a content in the different types of biomass can be determined or checked for foreign and / or pollutants. A central program control is provided, to which the values ascertained with the at least one analysis system can be transferred.

In the plant for hydrothermal carbonation, at least one reaction product can be adjusted by way of a mixed biomass leaving the mixer with regard to the percentage proportions of the different types of biomass, that in a reactor the at least one reaction product formed contains a predefined fraction of foreign substances and / or pollutants ,

For the production of carbon-containing reaction products from biomass by means of hydrothermal carbonization, the system (first area) is used to provide, comminute and mix the different types of biomass. In a second area, a preparation and preparation of the mixed biomass is carried out. In a third area, the reaction process of the hydrothermal carbonization is carried out. In at least a fourth area, further processing of the reaction products of the reaction process takes place.

In the third area, at least three reactors are provided for the production of carbonaceous products from biomass by hydrothermal carbonation. Each reactor has a first inlet at the top of the reactor for a first conduit, at least one outlet at the bottom of the reactor for a third conduit, and a second inlet at the top of the reactor. The second inlet is connectable controlled with the outlet via a second line. The second line is provided with a heat exchanger and a pump, whereby a solid / liquid mixture in the reactor can be circulated via the outlet and the second inlet.

A program control which detects the values of the at least one analysis system by means of which the content of foreign substances and / or pollutants in the different types of biomass can be determined is provided. Likewise, the process parameters are detected by a plurality of sensors associated with the reactor. Thus, the system and the reactor are controlled so that the content of foreign and / or pollutants in the reaction product is defined adjustable.

The first conduit system, the second conduit system and the third conduit system are provided with a plurality of controllable two-way valves and a plurality of controllable three-way valves which are connected to the program control, so that the specific filling, recirculation and emptying the at least three reactors can be controlled and controlled.

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. 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.

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 to 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. At least a portion of the reaction products from the at least one active reactor may be fed directly to the fifth region. 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 regulating 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 by suitable Program control possible to adjust the reaction product to the needs of a customer so that the fuel during combustion is an optimal performance. 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 can be made available. 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.

• • dass Biomasse unterschiedlichen Typs in einer Vielzahl von Annahme- und Lagerstellen bereitgestellt wird;
• • dass jeder Annahme- und Lagerstelle ein Analysesystem zugeordnet werden kann, mittels der ein Gehalt von Fremd- und/oder Schadstoffen in den unterschiedlichen Typen der Biomasse bestimmt und/oder überprüft wird; und
• • dass an eine Programmsteuerung die mit dem Analysesystem ermittelten Werte und ebenfalls die Prozessparameter von mehreren einem Reaktor zugeordneten Sensoren übergeben werden, so dass in einem System die unterschiedlichen Typen von Biomasse in einem Mischer zu einer homogenen Mischung aus mindestens zwei der unterschiedlichen Typen von Biomasse zusammengestellt werden und der Reaktor (301) derart gesteuert wird, dass der Gehalt von Fremd- und/oder Schadstoffen im Reaktionsprodukt definiert eingestellt wird.

The method for providing a mixture of different types of biomass for a hydrothermal carbonization plant comprises the following steps:

• • that biomass of different types is provided in a variety of acceptance and storage sites;
• • that each acceptance and storage site can be assigned an analysis system by means of which a content of foreign substances and / or pollutants in the different types of biomass is determined and / or verified; and
• • that the values determined by the analysis system and also the process parameters of several sensors assigned to a reactor are transferred to a program controller, so that in a system the different types of biomass in a mixer are combined to form a homogeneous mixture of at least two of the different types of biomass and the reactor ( 301 ) Is controlled so that the content of foreign and / or pollutants in the reaction product is set defined.

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. In the further drying of 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.

1 shows a schematic representation of the system according to the invention for carrying out the hydrothermal carbonization.

2 shows a schematic representation of another embodiment for carrying out the reaction process of the hydrothermal carbonization.

3 shows a further embodiment of the system for carrying out the reaction process of the hydrothermal carbonization.

4 shows a schematic representation of the first portion of the plant for hydrothermal carbonization, in which the necessary for the reaction process different biomass can be crushed and mixed.

5 shows a schematic representation of the second portion of the plant for hydrothermal carbonization, in which the crushed and mixed biomass with process water and catalyst are added before they are fed to the reaction process.

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

7 shows a schematic representation of the elements of the fourth area of the plant for hydrothermal carbonization, in which ultimately the reaction products are processed for further consumption.

8th shows a schematic representation of a reactor in conjunction with an associated heat exchanger.

9 shows a schematic representation of the system according to the invention for carrying out a reaction process for the production of biogas.

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. Although the following description of the 1 to 8th This is not to be construed as a limitation on the invention as it relates essentially to the hydrothermal carbonation reaction process. It is self-evident to a person skilled in the art that the principle of the invention provides for the targeted provision of the different types of biomass 51 . 52 , ..., 5n can be used to adjust a content of foreign and / or pollutants in the recovered reaction product. So z. B. also the content of foreign and / or pollutants in biogas can be adjusted.

1 shows the schematic structure of the plant 1 for hydrothermal carbonization. At the in 1 embodiment shown is the plant 1 for hydrothermal carbonation from a first area 100 , a second area 200 , a third area 300 and a fourth area 400 educated. The first area 100 , the second area 200 , the third area 300 and the fourth area 400 are by means of a common program control 10 connected. In the first area 100 the assembly and mixing of the different biomass takes place. From the first area 100 the mixed and shredded biomasses reach the second area 200 in which a processing and preparation of the mixed biomass is carried out. Process water PW is added to the crushed and mixed biomasses. From the second area 200 In this way, the biomass mixed with process water PW reaches the reactor area, which is referred to as the third area. 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.

2 shows a further embodiment of the system 1 for the hydrothermal carbonization of biomass. Here is the fourth area against a fifth area 500 replaced. 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 area 500 a reaction process is carried out in which synthesis gas is generated. To produce the synthesis gas, carbon dioxide CO _{2 is} fed in the fifth region. The supplied carbon dioxide may, for. B. from a carbon dioxide source 15 come. A carbon dioxide source 15 is z. Thus, directly from the fossil power plant formed and formed carbon dioxide to the process for synthesis gas production in the fifth area 500 the plant 1 be supplied.

3 shows a further embodiment of the invention. Here is in addition to the fourth area 400 the fifth area 500 intended. Part of the finished reaction products thus becomes the fourth region from the third region 400 fed. Thus, in the fourth area, the description already appears in the description 1 mentioned dewatering and drying of the reaction products. The thus obtained process water is from the fourth area 400 again the second area 200 fed. Another part of the reaction products from the third area 300 can the fifth area 500 be fed, in the end, with the addition of carbon dioxide from a carbon dioxide source 15 Synthesis gas is generated.

Analogous to the description of the 1 is also the embodiments of the in the 2 and 3 mentioned plants a program control 10 assigned over the material flow in various embodiments of the system 1 can be controlled and regulated.

4 shows a schematic representation of the system 100 which is the first area of the plant 1 forms, for the hydrothermal carbonization of biomass. The first area comprises a large number of acceptance and storage locations 121 . 122 , ..., 12n for the different types of biomass 51 . 52 , ..., 5n , In the 4 illustrated embodiment of the area 100 represents only one possible form of embodiment and should not be construed as a limitation. It is self-evident for a person skilled in the art that, depending on the customer requirement, the first area 100 can be designed. The number of acceptance and storage locations 121 . 122 , ..., 12n , depends on the different types of biomass used in the plant 1 to be processed. Likewise, the number of shredding units 13 depending on the type of biomass used with the plant 1 should be processed. After the appropriate comminution of the biomass these become a mixer 14 fed in which the mixed biomass 5 M is provided for the further reaction process. At the in 4 embodiment shown is each acceptance and storage 121 . 122 , ..., 12n is an analysis system 15 assigned by means of which a content in the different types of biomass 51 . 52 , ..., 5n can be determined or checked on foreign and / or pollutants. A central program control 10 become those with the respective analysis system 15 passed values. The double arrows shown in Figure between the individual acceptance and storage locations 121 . 122 , ..., 12n for the different types of biomass 51 . 52 , ..., 5n should imply that each acceptance and storage place 121 . 122 , ..., 12n on demand an analysis system 15 can be assigned.

At the in 4 shown embodiment of the first area 100 is a first crushing unit 131 and a second crushing unit 132 intended. The first shredding unit 131 is designed as a crusher. The second shredding unit 132 is designed as a hammer mill. The first shredding unit 131 Consequently, large pieces of biomass are supplied, which still require a strong crushing before they are fed to the mixer. The second shredding unit 132 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 these directly to the mixer 14 respectively. Likewise, in the embodiment of the 4 an acceptance and depository 123 for already liquid biomass. This liquid biomass can z. B. sewage sludge. The one with the first shredding unit 131 comminuted biomass is thus a supply of liquid biomass from the receiving and storage 123 fed. Thus, the from the first crushing unit 131 Biomass already mixed with a liquid biomass before this in the mixer 14 arrives. From the mixer 14 The biomass passes through a pipe 111 in the second area 200 , The second area 200 the plant 1 includes a mixing container 21 , In the mixing container 21 is one about a motor 221 driven stirring 220 intended. In the mixing container 21 gets over the line 111 the mixed biomass 5 M , Parallel to this is the mixing container 21 over a line 211 Process water PW supplied. In the line 211 for the process water PW is a mixer 214 inserted. Before the process water PW over the line 211 gets into the mixer, flows into the pipe 211 a line 212 , which in the process water a catalyst from a tank 213 supplies. The catalyst may, for. For example, formic acid, citric acid or sulfuric acid. After in the mixing container 21 the mixed biomass 5N and the process water PW are sufficiently mixed, the mixture thus obtained, which has a dry matter content of 20% to 60%, via a line 222 , which with a pump 30 is provided, the third area 300 fed.

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

The construction of the third area 300 is in 6 shown schematically. The third area 300 includes at least three reactors 301 , Each of the reactors is equipped with a positive pressure line 302 provided in a controllable two-way valve 32 ends. About this controllable two-way valve 32 Thus, the pressure inside the reactor can 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 the plant 1 need at least three reactors 301 be present to ensure continuous production of the reaction products of the hydrothermal carbonation process. At least one reactor 301 the reactors is an active reactor 301A , The term "active reactor" means that in this reactor 301 The process of hydrothermal carbonation is ongoing and not yet completed.

In at least one other reactor 301 The at least three reactors will be biomass via a pipe 311 in the reactor 301 filled. This reactor 301 becomes a refillable reactor 301F designated. At the in 6 shown schematic representation of the third area 300 the plant 1 are two refillable reactors 301F intended. The fillable reactors 301F be over the line 311 filled with the mixed with process water and catalyst biomass. In the line 311 is a first heat exchanger 310 brought in. Furthermore, the line connects 311 all reactors 301 of the third area 300 , Via a controllable three-way valve 33 can thus the line 311 in the direction of the at least one refillable reactor 300F be unlocked so that the reactor 301F can be filled with biomass, process water and catalyst.

Furthermore, a second conduit system 321 provided that also every reactor 301 of the third area 300 connects with each other. The second line 321 is designed as a loop and is also via a second heat exchanger 320 guided. Further, in the line 321 a pump 30 provided with the biomass from the at least one active reactor 301A constantly over the second heat exchanger 320 is pumped around. Through this pumping to achieve a constant mixing of the biomass in the active reactor 301A , In the form of a ring line second line 321 are several three-way valves 33 and two-way valves 32 provided, thus the material flow of just in the active reactor 301A Reactive biomass via the loop 321 and to recycle 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 301A forms an open ring, allowing the pumping of the biomass during the reaction process in the active reactor 301A is possible.

At least one other reactor 301 of the reactors in the third area 300 is a currently empty reactor 301L , This straight empty reactor 301L was previously the active reactor 301A , after the reaction process in the active reactor 301A is completed, the reaction products can be removed from the reactor. The active reactor 301A then becomes the empty reactor 301L , Each of the reactors 301 is with a third line 321 connected via a third heat exchanger 320 is guided. In the third line 331 are also a variety of two-way valves 32 and three-way valves 33 provided, thus controlled the emptying reactor 301L with the third line 331 connect to. That from the empty reactor 301L withdrawn reaction product is by means of the third line 331 via a relaxation device 340 guided, so that the reaction products are brought substantially to an ambient pressure level. From the relaxation facility 340 the reaction products reach the fourth range 400 and / or in the fifth area 500 in which, as already mentioned, synthesis gas can be produced.

For the further description of the invention, reference is made to the fifth area 500 omitted, can be made in the synthesis gas from the reaction products in conjunction with carbon dioxide. In the description of the present invention now comes, as in 7 shown the reaction product via the line 331 in the fourth area and is there in a container 41 spent. In the collection container 41 is a stirrer 420 that with a motor 421 is driven, arranged. About a line 411 in which a pump and at least one controllable two-way valve 32 are provided, the reaction product is placed in a drainage device. The over the line 331 supplied reaction products have a dry matter content of about 10%. In the drainage facility 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 container 436 Too high, the excess process water PW will overflow 437 delivered to the environment. About the line 311 , which with a pump 30 and a two-way valve 32 is provided, the process water PW in the second area 200 the plant 1 recycled. From the drainage facility 430 the reaction product enters a dryer 432 , The dryer is powered by a motor 433 driven. 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 enters a collection container 434 , From the collection container 434 Finally, the distribution to the consumers can be off with the plant 1 made reaction products.

8th shows a simplified schematic representation of the active reactor 301A in connection with the second line 321 , which is designed as a loop or switchable to a ring line. The loop is obtained by suitable control of two-way valves 32 and / or three-way valves 33 the plant 1 for hydrothermal carbonization. The second line 321 (or the controlled loop formed) comprises the second heat exchanger 320 , While in the active reactor 301 proceeding reaction process, the currently reacting biomass by means of a pump 30 and the second line 321 constantly over the second heat exchanger 320 circulated. Thus, one achieves a constant circulation in the active reactor 301 reacting biomass. In the active reactor 301 To initiate the reaction process, the filled biomass is brought to a certain temperature and pressure. During the pumping of the just reacting biomass via the second line 321 , is essentially the temperature and that in the active reactor 301A Maintaining prevailing pressure within a predefined range of fluctuation. By pumping the currently reacting biomass you save yourself mechanical components, with a passage in the reactor 301 or the other identical reactors 301 must be introduced. By pumping the reacting biomass in the active reactor 301 is thus a possible leakage over the implementation in the active reactor 301 avoided. This results in a much higher production reliability and susceptibility to interference with the system according to the invention.

In a plant 1 for charring biomass are at least three identical reactors 301 intended. Every reactor 301 for the production of carbonaceous products from biomass 51 . 52 , ..., 5n by hydrothermal carbonation has a stainless steel jacket. The reactor 301 has a first inlet 21 in the upper area 301o of the reactor 301 for a first line 311 , Furthermore, the reactor has 301 at least one outlet 23 in the area below 301U for a third line 331 formed, wherein the first line 311 and the third line 331 lead a solid / liquid mixture. The reactor 301 has a second inlet 22 in the upper area 301o of the reactor 301 and the second inlet 22 is with the outlet 23 over a second line 321 connected or within the plant 1 interconnected such that the second line 321 controlled inside the respective reactor 301 Reactive biomass from the outlet 23 to the second inlet 22 leads. The second line 321 is with a heat exchanger 320 and a pump 30 provided, whereby the solid / liquid mixture in the reactor 301 over the outlet 23 and the second inlet 22 can be circulated. Thus one achieves a constant movement and mixing of the biomass in the reactor 301 in which the reaction process takes place.

The reactor 301 are several sensors 25 associated with a variety of process parameters during the reaction process in the reactor 301 determine. The process parameters can be pressure, temperature, pH and / or level inside the reactor 301 etc. be. The measured values of the parameters are the program control 10 the plant 1 fed by means of controllable two-way valves 32 or three-way valves 33 a predefined pressure level inside the reactor ( 301 ) or the flow of material during the process of hydrothermal carbonization of biomass 51 . 52 , ..., 5n established.

At the in 5 shown embodiment of the system 1 are four identical reactors 301 shown. These reactors 301 can take on different functions depending on the end of the production process. So at least one reactor 301 the active reactor 301A be. When the reaction process is complete, the previously at least one active reactor becomes 301A the emptying reactor 301L , Is the at least one emptying reactor 301L completely emptied, the reactor becomes 301 to the fillable reactor 301F , The number of reactors 30 , the active reactors 301A or emptying reactors 301L or refillable reactors 301F are, according to the process conditions, to ensure a continuous output of reaction products from the plant 1 to ensure.

With the method according to the invention, it is possible to use a reaction product by means of the hydrothermal carbonization of different types of biomass 51 . 52 , ..., 5n manufacture. The reaction product is coal containing a predefined fraction of foreign and / or pollutants.

Furthermore, it is possible with the method according to the invention a reaction product by means of the hydrothermal carbonization of different types of biomass 51 . 52 , ..., 5n manufacture. The reaction product is synthesis gas containing a predefined fraction of foreign and / or pollutants.

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

9 shows a further embodiment for producing a reaction product by means of a reaction process. The reaction process in this case is the production of biogas from different types of biomass 51 . 52 , ..., 5n , The biomass 51 . 52 , ..., 5n will match the in 4 Scheme shown by means of the system according to the invention 100 compiled. The biomass mixed according to the specifications 51 . 52 , ..., 5n becomes the biogas reactor area 600 to hand over. The program control 10 Ensures that a correspondingly predefined content of foreign substances and / or pollutants is established in the reaction product biogas.

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.

QUOTES INCLUDE IN THE DESCRIPTION

This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Cited patent literature

• WO 2010006881 A1 [0007]
• DE 102008007791 A1 [0008]
• DE 102008028953 A1 [0009]
• WO 2008/120662 A1 [0010]
• DE 10200805844 A1 [0011]
• WO 2008/081407 A2 [0012]
• EP 1970431 A1 [0013]
• WO 2008/059989 A1 [0014]
• WO 2008/193309 [0015]
• EP 2130893 A2 [0016]
• EP 1762607 [0017]
• DE 20106837 U1 [0018]
• DE 19723510 C1 [0020]

Cited non-patent literature

• E. Behrl et al. (Ann. Chem. 493 (1932), pp. 97-123 [0006]
• Angew. Chemistry 45 (1932), pp. 517-519) [0006]
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• Wang et al., Carbon 39 (2001), pp. 2211-2214 [0006]
• X. San and Y. Li, Angew. Chem. Int. Ed. 43 (2004), pp. 597-601 [0006]

Claims (18)

System ( 100 ) for providing a mixture of different types of biomass ( 51 . 52 , ..., 5n ) for a plant ( 1 ) for the production of a reaction product by means of a reaction process, with a multiplicity of acceptance and storage sites ( 121 . 122 , ..., 12n ) for the different types of biomass ( 51 . 52 , ..., 5n ), at least one shredding unit ( 13 ) and a mixer ( 14 ), to create a homogeneous mixture of at least two of the different types of biomass ( 51 . 52 , ..., 5n ), characterized in that each receiving and storage point ( 121 . 122 , ..., 12n ) an analysis system ( 15 ), by means of which a content in the different types of biomass ( 51 . 52 , ..., 5n ) is determinable and / or verifiable to foreign and / or pollutants. System ( 100 ) according to claim 1, wherein a central program control ( 10 ) with which the analysis system ( 15 ) values can be transferred. System ( 100 ) according to claims 1 to 2, wherein in the annex ( 1 ) to at least one reaction product in such a way via a mixer ( 14 ), mixed biomass ( 5 M ) with regard to the percentage of different types of biomass ( 51 . 52 , ..., 5n ) that is adjustable in a reactor ( 301 ) contains at least one reaction product formed a predefined proportion of foreign and / or pollutants. System ( 100 ) according to claim 3, wherein the plurality of acceptance and storage locations ( 121 . 122 , ..., 12n ) and the predefined fraction of foreign and / or pollutants in the reaction product likewise by means of the 301 ) conditions of the reaction process can be influenced. System ( 100 ) according to one of claims 1 to 4, wherein a program control ( 10 ), which determines the values of the at least one analysis system ( 15 ) by which the content of foreign and / or pollutants in the different types of biomass ( 51 . 52 , ..., 5n ) and the process parameters of the reaction process and the system ( 100 ) controls such that the content of foreign and / or pollutants in the reaction product is defined adjustable. System ( 100 ) according to claims 1 to 5, wherein the reaction process comprises the production of biogas. System ( 100 ) according to claims 1 to 5, wherein the reaction process comprises the hydrothermal carbonization of biomass. System ( 100 ) according to claim 7, wherein for the production of carbonaceous products from biomass ( 51 . 52 , ..., 5n ) by hydrothermal carbonation in the system ( 100 ) providing, crushing and mixing the different types of biomass ( 51 . 52 , ..., 5n ), that in a second area ( 200 ) preparing and preparing the mixed biomass ( 5 M ) is feasible, that in a third area ( 300 ) the reaction process of the hydrothermal carbonization is executable and that in at least a fourth area ( 400 ) further processing of the reaction products of the reaction process is executable. System ( 100 ) according to claim 8, wherein in the third area ( 300 ) at least three reactors ( 301 ) for the production of carbonaceous products from biomass ( 51 . 52 , ..., 5n ) are provided by hydrothermal carbonation, each reactor ( 301 ) a first inlet ( 21 ) in the upper area ( 301o ) of the reactor ( 301 ) for a first line ( 311 ), at least one outlet ( 23 ) in the area below ( 301U ) of the reactor ( 301 ) for a third line ( 331 ) and a second inlet ( 22 ) in the upper area ( 301o ) of the reactor ( 301 ), wherein the second inlet ( 22 ) with the outlet ( 23 ) via a second line ( 321 ) is controllably connectable and that the second line ( 321 ) with a heat exchanger ( 320 ) and a pump ( 30 ), whereby a solid / liquid mixture in the reactor ( 301 ) over the outlet ( 23 ) and the second inlet ( 22 ) is umpumpbar. System ( 100 ) according to claims 8 and 9, wherein a program control ( 10 ), which determines the values of the at least one analysis system ( 15 ) by which the content of foreign and / or pollutants in the different types of biomass ( 51 . 52 , ..., 5n ) and the process parameters of several, the reactor ( 301 ) associated sensors ( 25 ) and the system ( 100 ) and the reactor ( 301 ) controls such that the content of foreign and / or pollutants in the reaction product is defined adjustable. System ( 100 ) according to claim 10, wherein the first conduit system ( 311 ), the second line system ( 321 ) and the third line system ( 331 ) with a plurality of controllable two-way valves ( 32 ) and a plurality of controllable three-way valves ( 33 ) provided with a program control ( 10 ), so that the specific filling, recirculation and emptying of the at least three reactors ( 301 ) is controllable and controllable. Method for providing a mixture of different types of biomass ( 51 . 52 , ..., 5n ) for a plant ( 1 ) for producing a reaction product by means of a Reaction process, characterized by the following steps: • that biomass ( 51 . 52 , ..., 5n ) of different types in a large number of acceptance and storage sites ( 121 . 122 , ..., 12n ) provided; • that each acceptance and storage point ( 121 . 122 , ..., 12n ) an analysis system ( 15 ) can be assigned if necessary, by means of which a content of foreign and / or pollutants in the different types of biomass ( 51 . 52 , ..., 5n ) is determined; and • that to a program control ( 10 ) with the at least one analysis system ( 15 ) and also the process parameters of several, one reactor ( 301 ) associated sensors ( 25 ), so that in one system ( 100 ) the different types of biomass ( 51 . 52 , ..., 5n ) in a mixer ( 14 ) to a homogeneous mixture of at least two of the different types of biomass ( 51 . 52 , ..., 5n ) and the reactor ( 301 ) Is controlled so that the content of foreign and / or pollutants in the reaction product is set defined. The method of claim 12, wherein the reaction process biogas is produced. The method of claim 12, wherein the reaction process, a hydrothermal carbonization of biomass is performed. The method of claim 14, wherein the program control ( 10 ) in the first system ( 100 ), in a second area ( 200 ), in a third area ( 300 ), in a fourth area ( 400 ) and / or in a fifth area ( 500 ) by a plurality of two-way valves ( 32 ), Three-way valves ( 33 ) and pumps ( 30 ), a material flow within the plant ( 1 ) via the program control ( 10 ) is regulated and that the predefined content of foreign and / or pollutants in the reaction product can be set defined. Method according to claim 15, wherein in the third area ( 300 ) at least three reactors ( 301 ) for the production of carbonaceous products from biomass ( 51 . 52 , ..., 5n ) are provided by hydrothermal carbonation, each reactor ( 301 ) a first inlet ( 21 ) in the upper area ( 301o ) of the reactor ( 301 ) for a first line ( 311 ), at least one outlet ( 23 ) in the area below ( 301U ) of the reactor ( 301 ) for a third line ( 331 ) and a second inlet ( 22 ) in the upper area ( 301o ) of the reactor ( 301 ), wherein the second inlet ( 22 ) with the outlet ( 23 ) via a second line ( 321 ) and that the second line ( 321 ) with a heat exchanger ( 320 ) and a pump ( 30 ), whereby a solid / liquid mixture in the reactor ( 301 ) over the outlet ( 23 ) and the second inlet ( 22 ) is circulated. Reaction product of the hydrothermal carbonization of different types of biomass ( 51 . 52 , ..., 5n ), wherein the reaction product is prepared by the process according to claims 12 to 16, characterized in that the reaction product is coal containing a predefined fraction of foreign and / or pollutants. Reaction product of the hydrothermal carbonization of different types of biomass ( 51 . 52 , ..., 5n ), wherein the reaction product is prepared by the method according to claims 12 to 16, characterized in that the reaction product is synthesis gas containing a predefined fraction of foreign and / or pollutants.

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