Method And Device For Producing Operating Materials Or Fuels

Abstract

The invention relates to a method and to devices for producing operating materials or fuels, humus, Maillard or similar reaction products from a solid-liquid mixture of water and a carbonaceous component and for treating said mixture, wherein the solid-liquid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar.

Description

BACKGROUND OF THE INVENTION

The application relates to a method and apparatus for the production of materials or fuels, humus, Maillard or Maillard-like reaction products from a solid-fluid mixture of water and a carbon-containing component and for the treatment thereof, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar.

1. State of the Art

In 1913, Friedrich Bergius described the production of coal from wood or cellulose at temperatures between 245 and approximately 340° C. with exclusion of air in a laboratory reactor without the use of catalysts for the first time in his postdoctoral document “the use of high pressures in chemical processes and a reproduction of the development process of coal”. The carbon contents measured in the elementary analysis were usually above 70 percent. A calculation of the exothermic reaction of cellulose carried out by Bergius in this process was essentially confirmed in July 2006 by Professor Markus Antonietti of the Max Planck Institute of Colloids and Interfaces in Potsdam, who introduced this method to the public in the laboratory scale with the name hydrothermal carbonization.

In this method, biomass is converted in a laboratory autoclave at 10 bar and 180° C. within half a day into a carbon-like material or its preliminary steps and water. The use of humid biomass for energy recovery through the production of a fuel which is as consistent as possible is aimed for a long time, but has been limited in its use up to now due to the lacking efficiency. Carbon dioxide emissions by combustion of fossil energy carriers are essentially seen to be responsible for the climate change.

In DE 19723510 for example, a device for the treatment of biogenous residues was presented which comprises a cylindrical reactor in which food waste and the like is submitted to a temperature pressure hydrolysis process or thermal pressure hydrolysis. The reactor is in the form of a loop reactor having heatable casing surfaces. A flow is produced within the reactor by means of a pump for ensuring mixing of the suspension.

2. Description of the Invention

It is the object of the invention to develop methods and devices, by means of which fuels, humus, carbon-containing materials as well as Maillard or Maillard-like reaction products can be manufactured economically and with high efficiency from a solid-fluid mixture, in particular, on an industrial scale. The object is achieved according to the invention by the objects of the independent claims. Advantageous further developments of the objects of the invention result from the dependent claims.

The object is solved by advantageous method for the hydrolysis and/or production of materials or fuels, humus, Maillard or Maillard-like reaction products from a solid-fluid mixture of water and a carbon-containing component and for the treatment thereof, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar in a reactor for at least 1 hour. According to the invention, feed materials that cannot be pumped are fed into the at least one reactor via a first feed strand, and pumpable heated feed materials are guided into the at least one reactor in a time-parallel manner or offset therefrom.

In an advantageous embodiment of the invention, it is thereby provided that non-pumpable feed materials with a solid content of 25 to 97 percent are conveyed to the reactor via the first feed strand and that parallel or offset thereto pumpable heated feed materials with a solid content of 3 to 50 percent are guided via the second feed strand. The ratio of the mass throughput of non-pumpable to pumpable feed materials is preferably 1:20 to 10:1.

In a further advantageous embodiment of the invention it is provided that the non-pumpable feed materials from the first feed strand are conveyed to the reactor under a pressure above the vapor pressure of the process water. The conveying device for introducing the non-pumpable feed materials form the first feed strand to the reactor under pressure above the vapor pressure of the process water is preferably an injector, double screw extruder, an eccentric spiral pump, a piston pump, a spiral displacement pump, which are respectively equipped with or without compressor screws, or a double screw compressor.

In an advantageous embodiment of the invention it is further provided that the non-pumpable feed materials from the first feed strand are provided to the reactor at a pressure below the vapor pressure of the process water and are superposed with pumpable feed materials from the second feed strand. The ratio of the mass throughput of provided vs. supplied feedstocks is preferably 1:20 to 10:1, or 1:5 to 1:1. According to the invention, further feed strands are preferably used in the method.

The method according to the invention further comprises the common use of further devices such as storage containers, comminution apparatuses, mixing vessels, dosing devices, incubation vessels, conveying devices, process water vessels, tube lines, heat exchangers or reactors.

In a further advantageous embodiment of the invention it is provided that the pump for conveying solid-fluid mixtures in the second feed strand is designed for sold contents of at least 5 to 10 or 10 to 25 percent. The pump for conveying solid-fluid mixtures in the second feed strand is for example an eccentric spiral pump, a spiral displacement pump, or a piston pump.

The object is also solved by a method for the hydrolysis of a carbon-containing component, for feeding a reactor and/or for producing materials or fuels, humus, Maillard or similar reaction products of a solid-fluid mixture of water and the carbon-containing component, where the solid-fluid mixture is treated at a temperature of above 100° C. and a pressure of above 5 bar. According to the invention, the solid-fluid mixture thereby flows through a heat exchanger for heating, where the amount of the angle of the tube axis to the horizontal plane is larger than 10 degrees. The viscosity of the solid-fluid mixture thereby for example decreases when passing through the feeding device and is for example reduced to at least three quarters of the viscosity of the feed materail at the end of the process.

In an advantageous embodiment of the invention it is provided that the solid-fluid mixture flows through a heat exchanger for heating and is thereby guided through at least 60 percent of essentially vertical tube parts. The solid-fluid mixture has for example a solid content between 3 and 35 or between 35 and 60% and/or is preferably guided to the heat exchanger by a pump. The pump for conveying the solid-fluid mixture and/or a counterpressure pump can for example be designed for solid contents of at least 5 to 10 or 10 to 25 percent and/or be an eccentric spiral pump, a spiral displacement pump, or a piston pump.

The object is further solved by an apparatus for treating a solid-fluid mixture of water and a carbon-containing component at a temperature above 100° C. and a pressure above 5 bar gelöst, which comprises a reactor and a feed apparatus. The feed apparatus comprises a pump according to the invention for conveying solid-fluid mixtures with a solid content of at least 10 or at least 15 mass percent or a heat exchanger, where the amount of the angle of the tube axis to the horizontal plane is larger than 10 degrees.

The object is further alternatively solved by an apparatus for treating a solid-fluid mixture of water and a carbon-containing component at a temperature above 100° C. and a pressure above 5 bar, which comprises a reactor and a hydrloysis apparatus. The hydrolysis apparatus comprises a pump according to the invention for conveying solid-fluid mixtures with a solid content of at least 10 or at least 15 mass percent or a heat exchanger, where the amount of the angle of the tube axis to the horizontal plane is larger than 10 degrees. The hydrolysis apparatus can for example comprise a counterpressure pump.

In an advantageous embodiment of these devices according to the invention it is provided that the pump is an eccentric spiral pump or a piston pump. The pump is thereby preferably designed for pressures of 10-130 bar.

In a further advantageous embodiment of the apparatuses according to the invention, it is provided that the heat exchanger consists of at least 60% of vertical tube parts. The heat exchanger can further be designed for passing through solid-fluid mixtures with a solid content of 3 to 50% essentially consisting of biomass including ligno cellulose and/or starch-containing material. The heat exchanger is preferably designed for temperatures of 60 to 300° C., at least one module or a unit for of the heat exchanger for temperatures of 200 to 300° C., and/or for pressures of 10 to 120 bar, at least one module of a unit of the heat exchanger for pressures of 60 to 120 bar. In an advantageous embodiment of the invention the heat exchanger or at least one module or a unit is designed for temperatures for up to 250° C.

In a further advantageous embodiment of the apparatuses according to the invention, it is provided that media-contacted tubes of the heat exchanger consist of heat and corrosion-resistant and water-repellant material, for example of coated metal, noble metal, ceramic materials or enamel. Media-contacting tubes of the heat exchanger thereby preferably consist of a corrosion-resistant material and/or of stainless steel as e.g. austenitic steel or steel with increasing chromium and molybdenum contents of the groups 6, 7 and 8, or of duplex steel, or of copper nickel alloy, high molybdenum-containing nickel ally or titanium.

In a further advantageous embodiment of the apparatuses according to the invention, it is provided that the heat exchanger is a tube reactor with a tempering system, a double tube heat exchanger, a tube bundle or a plate heat exchanger or a combination thereof. The heat exchanger preferably consists of several similar units and/or has a modular construction, wherein the similar units of the heat exchanger are arranged in a spatial vicinity to each other.

In a further advantageous embodiment of the apparatuses according to the invention, it is provided that a tempering system of a tube reactor consists of a double wall, wherein the intermediate space of the double wall of the tube reactor is flown through by a heat energy carrier medium. The heat energy carrier medium is thereby preferably a thermal oil, water vapor or process water, wherein the heat exchanger can be designed for different heat energy carrier media and/or for a target temperature of the heat energy carrier medium of 60 and 350° C. The heat exchanger preferably consists of different modules, units or sections.

The object is further alternatively solved by an apparatus for treating a solid-fluid mixture of water and a carbon-containing component at a temperature above 100° C. and a pressure above 5 bar, which comprises a reactor and a feed apparatus and/or a hydrolysis apparatus, wherein the feed apparatus and/or the hydrolysis apparatus comprises/comprise the following devices:a pump for conveying solid-fluid mixtures with a solid content of at least 10 to 15 percent and/or a heat exchanger, where the amount of the angle of the tube axis to the horizontal plane is larger than 10 degrees.

In an advantageous embodiment of the apparatus according to the invention it is provided that the hydrolysis apparatus has a counter pressure pump. In a further advantageous embodiment of the invention it is provided that the pump for conveying solid-fluid mixtures and/or the counter pressure pump is an eccentric spiral pump, a spiral displacement pump or a piston pump.

In a further advantageous embodiment of the invention it is provided that the pump and/or the counter pressure pump is/are designed at least for pressures of 10-30 bar. The heat exchanger for passing through solid-fluid mixtures can consist of at least 60 percent of vertical tube parts and/or be designed for a solid content of 3 to 50 percent, wherein the solid content can essentially consist of biomass including lignocellulose and/or starch-containing material.

In a further advantageous embodiment of the invention it is provided that the heat exchanger is designed for temperatures of 60 to 300° C. or at least one module or a unit is designed for temperatures of 200 to 300° C. The heat exchanger or at least one module or a unit of the heat exchanger is preferably designed for pressures of 10 to 120 bar and in an advantageous embodiment of the invention for pressures of 60 to 120 bar, and/or for temperatures up to 250° C.

In an advantageous embodiment of the invention it is further provided that the media-contacting tubes of the heat exchanger consist of heat- and corrosion-resistant and water-repellant material, for example of coated metal, and in an advantageous embodiment of the invention noble metal, ceramic materials or enamel. The media-contacting tubes of the heat exchanger preferably consist of a corrosion-resistant material such as stainless steel including austenitic steels or steels with increasing chromium and molybdenum contents of the groups 6, 7 and 8 or also diplex steels, copper nickel alloys, high molybdenum-containing nickel alloys, as e.g. 2.4610, or titanium.

In a further advantageous embodiment of the invention it is provided that the heat exchanger is a tube reactor with a tempering system, a double tube heat exchanger, tube bundle or plate heat exchanger or a combination thereof.

The heat exchanger preferably consists of several similar units or has a modular construction, wherein the similar units of the heat exchanger are preferably connected in series and/or the modular units of the heat exchanger are arranged in a spatial vicinity to each other.

In a further advantageous embodiment of the invention it is provided that the tempering system of the tube reactor consists of a double wall, wherein the intermediate space of the double wall of the tube reactor can be flown through by a heat energy carrier medium. The heat energy carrier medium is thereby preferably a thermal oil, water vapor or process water, wherein the heat exchanger can be designed for different heat carrier media.

In a further advantageous embodiment of the invention it is provided that the heat exchanger is designed for a target temperature of the heat carrier medium of 60 to 350° C. The heat exchanger can also consist of different modules, units or sections.

The object is further solved by a method, where feed materials are supplied continuously to a first reactor via a heat exchanger over a period of at least six tenth of the reaction time, and the reaction mixture is guided in batch mode from one to the following reactor, wherein reaction products are discharged continuously from a last reactor over a period of at least six tenth of the reaction time. The essential steps of the method according to the invention are thus carried out continuously, wherein the period, via which feed materials are introduced over a reaction cycle or over the time necessary for a passage of the material into the process via the heat exchanger, is at least six tenth of the reaction cycle.

In an advantageous embodiment of the invention it is provided that one batch is at least 10 and up to 25 mass percent, or at least 25 mass percent of the reactor content of the respective previous reactor. A batch preferably remains in a closed reactor for avoiding back mixtures for a period of at least a hundredth of the reaction time, which reactor is positioned in the flow-through region behind at least the first reactor. The closure of the closed reactor can thereby be regulated via closure assemblies such as pressure valves or blocking flaps.

In a further advantageous embodiment of the invention it is provided that no more than 60 Vol-% of a batch is supplied to the closed reactor during the dwelling time. Batches with a remaining reaction time with a similar length are preferably combined from at least two reactors into the following reactor. The remaining reaction times of combined batches should thereby not deviate from each other by no more than 50 percent of the longest remaining reaction times of the combined batches.

In a further advantageous embodiment of the invention it is provided that the last reactor is a further heat exchanger. The further heat exchanger is preferably flown through by the feed materials for cooling the reaction mixture during at least six tenth of the reaction time. According to the invention, at least one heat exchanger can be a tube reactor with a tempering system, a double tube heat exchanger, a tube bundle or plate heat exchanger or a combination thereof.

In an advantageous embodiment of the invention it is further provided that the heat exchanger is flown through by the feed materials for heating the feed materials during at least six tenth of the reaction time. In a further advantageous embodiment of the invention it is provided that the reaction mixture is guided through a heat exchanger during the guiding from one reactor to the following one. The reaction mixture is preferably guided through the heat exchanger for devolatilization, wherein the heat exchanger is preferably flown through by reaction participants during at least six tenth of the reaction time for the devolatilization.

In a further advantageous embodiment of the invention it is provided that a heat exchanger consists of several similar units and/or has a modular construction, wherein the similar units of the heat exchanger can be connected in series. The modular units are preferably thereby arranged in a spatial vicinity to each other. A tempering system of a tube reactor preferably consists of a double wall, wherein the intermediate space of the double wall of the tube reactor can be flown through be a heat energy carrier medium. A thermal oil, water vapor or process water is thereby preferably used as the heat energy carrier medium, wherein different heat energy carrier media can be combined. The target temperature of the heat energy carrier medium by which the heat exchanger is flown through, is preferably between 60 and 350° C.

In a further preferred embodiment of the method according to the invention, the heat exchanger consists of different modules, units or sections. The temperature in a first section or module of the heat exchanger is for example at 60-100 or 80-120° C., in a second section or module between 100 and 140 or between 120 and 160° C., in a third section between 140 and 180 or between 160 and 200° C. and in a fourth section between 180 and 220, between 200 and 240 or between 240 and 350° C. The units, modules or sections of the heat exchanger can thereby be connected in series in such a manner that the temperature of the solid-fluid mixture is again brought to a lower inlet or outlet temperature after reaching a highest or peak temperature of for example 220 to 260° C.

In a further advantageous embodiment of the invention it is provided that the heat exchanger is equipped with a holding path, by which the temperature is kept on an even level of for example +/−2 to 80° C. Preferred according to the invention, the reaction mixture is guided into at least one reactor equipped with a stirring or mixing system after passing through the heat exchanger for mixing or swirling, or into a reactor whose height is at least double of its diameter.

In a further advantageous embodiment of the invention it is further provided that the components consist of feed materials, water or catalysts.

During the dwelling time of a batch in a reactor, components, reaction products, process water or catalysts are preferably withdrawn, wherein the period over which the components, reaction products, process water or catalysts are withdrawn ids at least preferably one hundredth of the dwelling time. During the dwelling time of a batch in the reactor, components, process water or catalysts can also be supplied for a period of at least one hundredth of the dwelling time. Supplied process water is thereby preferably treated, wherein the treatment of the supplied process water can comprise at least one solid-fluid separation or another water reconditioning measure.

In a further advantageous embodiment of the invention it is provided that the method takes place under oxygen closure. The treatment of the solid-fluid mixture consisting of water and the carbon-containing component is preferably a hydrolysis. The object is further solved by an apparatus for the production of materials or fuels, humus, Maillard or Maillard-like reaction products of a solid-fluid mixture of water and a carbon-containing component, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar, and water is withdrawn continuously or in intervals from the solid-fluid mixture in a membrane reactor during the reaction. The membrane reactor thereby preferably has at least one apparatus for the solid-fluid separation, which comprises at least one coarse and/or a fine filtration of a combination of both apparatuses, which can also be combined in a filtration device. By the use of the membrane reactor, reaction, intermediate, secondary and end products can selectively be removed from the reaction mixture, educts can be added or removed in a controlled manner or the contact of the educts can be intensified. The solid-fluid separation of the membrane reactor proceeds for example continuously or in intervals.

The object is further solved by a method for the production of materials or fuels, humus, Maillard or Maillard-like reaction products of a solid-fluid mixture of water and a carbon-containing component, and for the treatment thereof, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar. According to the invention, reconditioned process water is partially used for preincubation, preheating of feed materials, production of the pumpability of a solid-fluid mixture, for reception in the reaction mixture, for overcoating or for the admixing to provided feed materials in a reactor of the plant, for the return in the running process, as heat carrier medium e.g. for further processes within or outside a plant and/or is used as a fertilizer component.

The reconditioning is preferably carried out by means of solid-liquid separation and/or carried out by evaporating water. Thereby, at least 1 to 10%, or more than 10% of the water are removed thereby. In an advantageous embodiment of the invention it is provided that the process water is taken either directly from the running process or from an insulated reservoir and which is designed as a pressure vessel for untreated process water for the reconditioning. In an advantageous embodiment of the method of the invention it is further provided that the water vapor obtained from the evaporation of the process water is used at a different location in the process, as for example for heating the feed materials prior to the entry into a heat exchanger, heating of thermal oil via a heat exchanger process and/or for operating an apparatus for drying reaction products as e.g. an air swirling mill.

The use of reconditioned process water of a method for the production of materials or fuels, humus, Maillard or Maillard-like reaction products of a solid-fluid mixture of water and a carbon-containing component, is also used according to the invention, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar, for the preincubation, preheating of feed materials, production of a pumpable solid-fluid mixture, for the reception in the reaction mixture, for the overcoating or for the admixing of provided feed material in a reactor of the plant, for returning into the running process, as heat energy carrier medium or as a fertilizer component. The process water can thereby be obtained at temperatures of 1 to 50° C. above the temperature for the respective use. Preferably, heated process water with a temperature of 25 to 50, 50-70 or 70-99° C. is used.

The object is also solved by an apparatus for the production of materials or fuels, humus, Maillard or Maillard-like reaction products of a solid-fluid mixture of water and a carbon-containing component, and for the treatment thereof, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar, which comprises according to the invention an apparatus for the reconditioning of withdrawn process water and for returning the reconditioned process water to the solid-fluid mixture. The apparatus preferably comprises an apparatus for the solid-fluid separation and an evaporator. In an advantageous embodiment of the invention, the apparatus can also comprise an insulated reservoir and which is designed as a pressure vessel for untreated process water.

The object is further solved by a pumpable fuel suspension or dispersion, which was produced from a solid-fluid mixture of water and a carbon-containing component by treatment at a temperature of above 100° C. and a pressure of above 5 bar according to the above-described method. According to the invention, the suspension or the dispersion has a solid content of at least 40%, wherein the solid content has a carbon content of at least 50%. The object is also solved by an additional suspension or dispersion for the production of ceramic materials, which was produced from a solid-fluid mixture of water and a carbon-containing component by treatment at a temperature of above 100° C. and a pressure of above 5 bar according to the above-described method. According to the invention, the suspension or the dispersion has a solid content of at least 50%.

The additional material suspension or dispersion according to the invention is preferably used for the production of ceramic materials in a sol-gel method, wherein this use comprises the adding of the acidic suspension to an alkaline sol and thus the initiation of the gelating process. The use of a solid-fluid mixture of water and a carbon-containing component as feed or additional material for the production of an insulating and/or ceramic material is also claimed according to the invention, wherein the solid-fluid mixture is treated at a temperature of above 100° C. and a pressure of above 5 bar and the sulfur and/or ash content of the solid-fluid mixture is reduced by at least 50% or 75% with regard to the respective original content of the carbon-containing component. In an advantageous embodiment of this use according to the invention, it is provided that the mixture is acidic and a ceramic material is produced by means of an alkaline sol.

In an advantageous embodiment of the mentioned uses according to the invention it is provided that the material is a silicium compound and the sol contains organic or inorganic silicates and/or silicon dioxide. The sol is thereby preferably an aqueous solution of water glass. The uses further comprise the production of a gel containing a carbon component and a silicate component and the heating of the gel up to the development of SiC gas. The uses according to the invention also comprise the production of the ceramic material while using the SiC gas, wherein the SiC gas can penetrate a provided porous forming body. This porous forming body preferably contains graphite. The produced material can for example be a silicium carbide such asSiC or SiSiC.

The object is further solved by a method for the production of materials or fuels, humus, Maillard or Maillard-like reaction products, which comprises the treatment of a solid-fluid mixture of water and a carbon-containing component, e.g. biomass, at a temperature of over 100° C. and a pressure of over 5 bar. According to the invention, it is thereby provided that the treatment is carried out in a continuous manner, in order to enable in an efficient, fast and cost-efficient method progress.

In an advantageous embodiment of this method according to the invention, it is provided that the treatment last for at least one hour (1 h) and/or comprises a processing of the biomass and/or a reconditioning of the reaction, intermediate, secondary and/or end products. The temperature is preferably adjusted to above 160° C., preferably between 160 and 300° C. or between 185 and 225° C., and/or is controlled automatically.

In an advantageous embodiment of the invention the pressure is adjusted to at least 7 bar, between 10 and 34 bar, 10 and 17 bar, 18 and 26 bar or 27 and 34 bar. The treatment duration can for example be at least 2 hours, 3 to 60 hours, 5 to 30 hours or 31 to 60 hours, 6 to 12 hours or 12 to 24 hours, wherein the treatment duration is preferably chosen in dependence on the type of biomass and/or the desired reaction product.

In an advantageous embodiment of the method according to the invention, it is further provided that the biomass is pretreated, preferably be dewatering, comminution, preincubation with auxiliary materials, mixing and/or preheating. The biomass is thereby incubated prior to the treatment at an acidic pH value. The pH value can thereby for example be below 6, below 5, below 4, below 3 or below 2.

In an advantageous embodiment of the method according to the invention, it is further provided that the biomass is comminuted prior to, during and/or after the treatment, preferably chaffed and/or milled. The particle size of the comminuted biomass is thereby below 10 cm, below 1 cm or below 2 mm.

In a further advantageous embodiment of the method according to the invention it is provided that at least one catalyst is added to the biomass prior to or during the treatment. The catalyst can be composed of several components, which together form a catalyst mixture. The catalyst is preferably an inorganic acid, preferably sulfuric acid and/or a mono, di- or tricarbonic acid, preferably tartaric acid or citric acid. The acid used as catalyst can simultaneously also be used for adjusting the pH value for the incubation step. The catalyst can comprise one or several metals and/or metal compounds, wherein the metal, the metals and the metal connections comprises/comprise at least one transition metal of the secondary groups Ia, IIa, IVa, Va, VIa, VIIa and Villa of the periodic system. The catalyst preferably comprises at least one biocatalyst, preferably enzymes, micro organisms, plant cells, animal cells, and/or cell extracts.

In an advantageous embodiment of the method according to the invention, it is further provided that the biomass is mixed prior to or during the treatment, preferably by stirring, mixing, suspending and/or swirling, wherein one or several mixing devices, preferably a liquid jet mixer, pump or nozzle can be used for mixing. In a further advantageous embodiment of the method according to the invention it is provided that the reaction products are dried with a drier after the treatment, preferably a convection or contact drier, with a with a flow and/or belt, and/or a fluidized bed drier.

Preferably according to the invention, process water accumulated during the course of the method is preferably withdrawn through at least one apparatus for solid-fluid separation and or cleaned and fed back to the reaction mixture. The apparatus for the solid-fluid separation can thereby be at least one apparatus for the micro-, ultra-, nanofiltration and for the reverse osmosis method or a combination of different above-mention apparatuses, with ceramic filter elements and in an advantageous embodiment a rotation disk and/or a centrifugal membrane filter.

In an advantageous embodiment of the method according to the invention, it is further provided that accumulated waste water is cleaned mechanically, chemically and/or biologically.

In a further advantageous embodiment of the method according to the invention it is provided that the reaction, intermediate, secondary and/or end products comprise fuels from peat to lignite to black coal-like fuels, humus, Maillard- or Maillard-like reaction products, carbon-containing materials such as insulating materials, nano-sponges, pellets, fibers, cables, active or sorption coal, charcoal substitute material, highly compacted carbon products and materials, and also feed materials for graphite and graphite-containing or -like products and carbon fibers and feed materials for composite and fiber composite materials.

The object is also solved by a plant for the production of materials or fuels, humus, Maillard or Maillard-like reaction products from a solid-fluid mixture of water and a carbon-containing component and for the treatment thereof at a temperature of over 100° C. and a pressure of over 5 bar, which comprises the following devices: a feeding device comprising a pump for conveying solid-fluid mixtures with a solid content of at least 10 to 15%, and/or a heat exchanger, where the amount of the angle of the tube axis to the horizontal plane is larger than 10 degrees; and/or at least two reactors, of which at least one is equipped with a stirring or mixing system or has a height-diameter-ratio of at least 2:1.

The heat exchanger of the plant has the above-described characteristics. The plant according to the invention further preferably has a devolatilization apparatus, wherein the devolatilization can comprise a reactor with a tempering system or a heat exchanger or a combination of both. The object is further solved by a method for the production of materials or fuels, humus, Maillard or Maillard-like reaction products from a solid-fluid mixture of water and a carbon-containing component, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar, wherein the solid-fluid mixture passes through at least two reactors connected in parallel and at least one reactor connected upstream and/or at least one reactor connected downstream.

According to the invention, the solid-fluid mixture is preferably heated, comminuted, mixed and/or swirled in at least one reactor connected upstream. In a further advantageous embodiment of the method according to the invention, the solid-fluid mixture is treated chemically in at least one reactor connected upstream, preferably adjusted to a certain pH value, and/or reconditioned in at least one reactor connected upstream, preferably by withdrawing liquid.

In a further advantageous embodiment the solid-fluid mixture is devolatized in at least one reactor connected downstream, preferably by cooling the mixture, and/or is heated, comminuted, mixed and/or swirled in at least one reactor connected downstream. The solid-fluid mixture can further also be treated chemically in at least one reactor connected downstream, preferably adjusted to a certain pH value. The solid-fluid mixture can however also be reconditioned in a reactor connected downstream, preferably by withdrawing liquid.

The object is also solved by an apparatus for the treatment of a solid-fluid mixture of water and a carbon-containing component at a temperature above 100° C. and a pressure above 5 bar, which comprises a first reactor and at least one further reactor, wherein the further reactor is connected in parallel to the first reactor and wherein at least one reactor connected downstream is connected in parallel to the first reactor and wherein at least one reactor connected upstream and/or at least one reactor connected downstream is/are provided.

The reactor connected upstream is preferably a tube reactor, a membrane reactor and/or a reactor, which comprises at least one vertical basic body. The reactor connected downstream is preferably also a tube reactor, a membrane reactor and/or a reactor, which comprises at least one vertical basic body. The height-diameter ratio of the cylindrical basic body is preferably 1:0.5, 1:2, 1:5 or lower.

In an advantageous embodiment of the invention, the reactor connected downstream has a different volume than the first reactor, preferably a larger volume for the devolatilization of the solid-fluid mixture. The mixture in the reactor connected downstream is additionally cooled for the devolatilization. In a further advantageous embodiment of the invention it is provided that the reactor connected downstream has a lower wall thickness than the first reactor.

The object is further solved by a method for the production of materials or fuels, humus, Maillard or Maillard-like reaction products from a solid-fluid mixture of water and a carbon-containing component, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar. According to the invention, the solid-fluid mixture is supplied continuously to at least one first reactor, treated in at least one second reactor and is withdrawn from at least one third reactor.

In an advantageous embodiment of the invention it is provided that the supply, treatment and withdrawal of the solid-fluid mixture in the individual reactors take place at the same time.

Preferably, at least one parallel reactor is provided, which is connected in parallel to at least one of the first, second and/or third reactors, in which the supply, treating and/or withdrawal takes place at the same time.

The solid-fluid mixture is preferably heated, comminuted, mixed and/or swirled in at least a first and/or third reactor. Alternatively or additionally, the solid-fluid mixture can also be treated chemically in at least one first and/or third reactor, preferably adjusted to a certain pH value.

In a further advantageous embodiment of the invention it is provided that the solid-fluid mixture is reconditioned in at least one first and/or third reactor, preferably by withdrawing fluid. The solid-fluid mixture is preferably devolatized then in at least a third reactor, preferably by cooling.

The object is also solved by a device for treating a solid-fluid mixture of water and a carbon-containing component at a temperature of above 100° C. and a pressure of above 5 bar, which comprises at least three reactors, wherein at least one first reactor is provided for receiving the solid-fluid mixture, at least one second reactor for treating the solid-fluid mixture and at least one third reactor for removing the solid-fluid mixture.

Preferably, at least one parallel reactor is provided thereby, which is connected in parallel with at least one of the first, second and/or third reactors. In an advantageous embodiment of the invention it is provided that the first reactor for receiving the solid-fluid mixture is a reactor connected upstream in the sense of the previous description. In an particularly advantageous embodiment of the invention it is further provided that the third reactor for removing the solid-fluid mixture is a reactor connected downstream in the sense of the previous description.

DESCRIPTION OF EXEMPLARY PREFERRED EMBODIMENTS OF THE INVENTION

An exemplary method according to the invention provides that the carbon-containing solid-fluid mixture and/or the feed material are additionally processed prior to and/or during the treatment, and/or the reaction, intermediate secondary and/or end products are conditioned or processed. By virtue of this purposeful preparation or pre-treatment of the solid-fluid mixture and the further processing of the solid liquid mixture during the treatment or the reaction process and/or the reprocessing of the reaction, intermediate, secondary and/or end products, the yield of fuel, humus, carbon-containing materials and/or Maillard or Maillard-like reaction products can be substantially increased in a cost-effective manner.

In the course of this energetic utilization of biomass, only so much carbon dioxide is set free into the atmosphere as was previously needed by the living plants for their growth. The use of fuels from biomass is thus carbon dioxide neutral and hence climate friendly. Furthermore, the production of humus, which is spread on agricultural effective areas for example, can serve as a CO₂-sink. Without such measures and without an increased energetic use of non-fossil fuels and renewable raw materials, climate protection targets such as those specified in the Kyoto agreement, will hardly be achieved.

With the methods and apparatuses according to the invention for the utilization of biomass for the production of fuels, the proportion of carbon, which is lost during the conversion process, is substantially smaller than with other methods. Little or no carbon is lost in the course of an orderly conversion process. The carbon loss is over 30 percent with alcoholic fermentation processes, about 50 percent with the conversion into biogas, about 70 percent for a wood carbonization process, and over 90 percent for a composting process. Thereby, carbon is released as carbon dioxide or also as methane, which are each regarded as greenhouse gases and being harmful to the climate. This is not the case with the method according to the invention.

The method according to the invention has a high degree of efficiency. By contrast, the alcoholic fermentation only has an estimated net efficiency with regard to the energy yield of three to five percent compared to the energy stored in the original biomass or educts. During the method in accordance with the application, no or only very little CO₂ is set free. In contrast, during the conversion of biomass into biogas, about half of the carbon released as CO₂. Moreover, only a few substrates are suitable for the economical operation of a biogas plant.

In contrast to most methods known for converting biomass into a fuel, the heat released during the process with the method according to the application can be used for other steps or procedures within the plant itself. One of the main challenges for the energetic utilization of biomass is its high moisture content. In the method of the application however, the presence of water is a prerequisite for the chemical conversion process. In summary, so far the methods applied to an industrial scale for the conversion of biomass into energy are however limited in their application by a lack of efficiency, lesser energetic usability and cost-efficiency.

When treating solid-fluid mixtures such as biomass for example at high temperatures and high pressures, the reactors in which the treatment takes place, can have special characteristics. Thus, the inner surface of the reactor can be corrosion-resistant or provided with an appropriate coating due to the extreme conditions. Moreover, a device for the mixing of the solid-fluid mixture can be provided.

The invention relates for example to a method for the production of materials and/or fuels, humus and/or Maillard and/or Maillard-like reaction products from carbon-containing solid-fluid mixtures, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar for a treatment period of at least 30 to 60 minutes. In a further embodiment of the object of the invention, the method is carried out in a semi-continuous or continuous manner. This means that the treatment of the solid-fluid mixture is not carried out in a discontinuous manner that is in a batch mode, in particular during the reaction process. Temperature and pressure ratios are mainly kept in the operating region for the optimizing reaction space usage and for minimizing the dwelling times. Simultaneously, feed materials and catalysts can be introduced into the reaction space in a time-delayed manner, process water and non-converted feed materials and other fed materials can be removed and be recycled according to requirement and contraries, reaction, intermediate, by and/or end products can be withdrawn. Parallel to this, further method steps, as for example the reconditioning and/or cleaning of process water, waste water, waste air, reaction, intermediate, by and/or end products is carried out continuously or in intervals.

In a further embodiment of the object of the application, it is provided that the temperature is adjusted to above 160° C., or between 160 and 300 ° C., or between 185 and 225° C., and/or that the temperature is controlled automatically. In a further embodiment of the object of the application, it is provided that the pressure is adjusted to above 7 bar, or between 10 and 34 bar, or between 10 and 17 bar, 17 and 26 bar or 26 and 34 bar. In a further embodiment of the object of the application, it is provided that the treatment duration is at least 30 to 60 minutes, 1-3, 3-6 or 6-24 hours, in some cases also 24-60 hours. In a further embodiment of the object of the application, it is provided that the treatment duration or conditions are chosen in dependence on the type of the feed material and/or the solid-fluid mixture and/or the desired reaction product.

In a further advantageous embodiment of the invention, it is provided that accumulated waste water is cleaned mechanically, chemically and/or biologically. In a further advantageous embodiment of the invention, it is provided that outlet air accumulated during the treatment, processing and/or conditioning is cleaned or treated mechanically, chemically and/or biologically.

In a further embodiment of the object of the application, it is provided that the solid-fluid mixture consists at least partially of biomass. The principle of the hydrothermal carbonization is thereby used by the supply of pressure and heat, so as to initially depolymerize and hydrolyze wet biomass while releasing heat energy in the efficient and highly economic method according to the application. The polymerization of the resulting monomers leads to the development of carbon-containing reaction products within a few hours. Desired reaction products are produced in dependence on the reaction conditions. After a shorter reaction duration, humus results initially among others, and, during the further course of the reaction, fuels with increasing carbon content, which are suitable for energy production.

The application also provides the production of different reaction, intermediate, secondary and/or end products according to the method of the application, including the production of fuels, from peat, and lignite to black coal-like fuels, humus, Maillard- or Maillard-like reaction products, carbon-containing materials such as insulating materials, nano sponges, pellets, fibers, cables, active or sorption coal, charcoal substitute material, highly compacted carbon products and materials, and in particular also feed materials for graphite and graphite-containing or -like products and carbon fibers and feed materials for composite and fiber composite materials.

In an exemplary embodiment of the object of the invention it is provided that the reactor is a cascade, tube, cycle reactor, loop and/or a stirring reactor and/or preferably a membrane and/or fluidized bed reactor. At least one reactor or a combination of different reactors preferably have at least one characteristic and preferably combinations of characteristics of a cascade, tube, cycle reactor, a loop or a stirring reactor, or of a membrane or fluidized bed reactor. At least one reactor comprises at least one membrane part and/or at least a device for the generation of a circulating fluidized bed layer.

In a further exemplary embodiment of the invention it is provided that it is provided that the apparatus for treating the biomass comprises at least one reactor for the reception of the biomass and at least a device for the processing of the biomass and/or conditioning of the reaction products and/or secondary products. In a further embodiment of the object of the application, it is provided that the reactor is a tubular reactor, cycle reactor, and especially advantageously a loop reactor or stirring reactor and/or preferably a membrane or fluidized bed reactor. At least one reactor preferably comprises at least one membrane part and/or at least a device for the generation of a circulating fluidized bed layer. At the same time, the reactor is designed for temperatures of at least 100° C., and at least a pressure of above 5 bar. Several reactors for the reception and treatment of the biomass can be provided to increase the capacity or the flow rate of the plant according to the invention. These can be connected in series.

The material and/or fuel according to the invention is produced from biomass and comprises, compared to biomass, a carbon fraction which is higher by 1 to 300 percent based on the percentage mass fraction of the elements (dry mass). The material and/or fuel according to the invention can comprise a carbon fraction increased by 10 to 300 percent, also 50 to 300 percent, or also 100 to 300 percent or 200 to 300 percent, compared to the biomass, based on the percentage mass fraction of the elements (dry mass). The material and/or fuel according to the invention can alternatively comprise a carbon fraction increased by 5 to 200 percent, also 10 to 150 percent, also 10 to 120 percent, and 50 to 100 percent, compared to the biomass, based on the percentage mass fraction of the elements (dry mass).

The material and/or fuel according to the invention comprises a carbon fraction compared to the feed material of 50 to 90 percent, also of 55 to 80 percent, and also of over 98 to percent, respectively based on the percentage mass fraction of the elements (dry mass). In a further embodiment of the object of the application, the hydrogen fraction of the material and/or fuel compared to the biomass is reduced by 1 to 300 percent, also 5 to 200 percent, and also 20 to 100 percent, respectively based on the percentage mass fraction of the elements (dry mass). In a further embodiment of the object of the application, the oxygen fraction of the material and/or fuel compared to the feed material is reduced by 1 to 300 percent, also 5 to 200 percent, and also 15 to 100 percent, respectively based on the percentage mass fraction of the elements (dry mass).

In a further embodiment of the object of the application, the nitrogen fraction of the material and/or fuel is reduced by 1 to 300 percent, 5 to 200 percent or 15 to 100 percent, respectively based on the percentage mass fraction of the elements (dry mass). The material and/or fuel according to the application can comprise at least or more than 65 percent of the original fuel value of the feed materials and in particular the biomass based on the dry mass.

The material and/or fuel according to the application can have, due to its composition and structure compared to the biomass or alternative fossil or biomass fuels, significantly more advantageous and environmentally friendly combustion characteristics, for example due to reduced ash parts, lower chlorine, nitrate, sulfur and heavy metal content, and lower emissions of dust or particulate matter, fine dust and gaseous toxic substances including nitrogen and sulfur oxides.

The material and/or fuel according to the invention can further also comprise a higher reactivity and a lower initiation temperature of combustion compared to the biomass or alternative solid fossil or biomass fuels. When the material and/or fuel according to the invention turns sufficiently porous, it can be comminuted with a lower energy expenditure than solid fossil fuels having a comparable fuel value or carbon content. A large surface results with a small particle size of the material and/or fuel according to the invention, in particular a particle size of about 2 nanometers to 50 micrometers, also below one micrometer, and also below 200 nanometer. The material and/or fuel according to the invention can then be dried easily due to the small particle size and its large surface.

The material and/or fuel according to the invention contains Maillard or Maillard-like reaction products. In one embodiment of the object of the application, the material and/or fuel of biomass is produced according to a method which comprises at least the following steps: the treatment of the biomass at a temperature of above 100° C. and a pressure of above 5 bar for a treatment duration of at least one hour and treatment of the biomass and/or conditioning of the reaction, intermediate, secondary and/or end products. The temperature can be adjusted to over 160° C., also between 160 and 300° C., and also between 185 and 225° C. The pressure can be adjusted to at least 7 bar, also between 10 and 34 bar, and also between 10 and 17 bar, 18 and 26 bar or 27 and 34 bar. The treatment duration is at least 2 hours, 3 to 60 hours, also 5 to 30 hours or 31 to 60 hours, 6 to 12 hours or 13 to 24 hours. After the treatment of the biomass, the reaction products are dried with a drier, also with a convection or contact drier, with a flow and/or belt, and/or with a fluidized bed drier up to a desired residual moisture content of 6 to 25 percent, also 10 to 20 percent, or also 12 to 15 percent.

The reaction, intermediate, secondary and end products of the method described above comprise fuels ranging from peat, and lignite to black coal-like fuels, humus, Maillard- or Maillard-like reaction products, and carbon-containing materials such as insulating materials, nano sponges, pellets, fibers, cables, active or sorption coal, charcoal substitute material, highly compacted carbon products and materials and in particular also feed materials for graphite and graphite-containing or -like products and carbon fibers and feed materials for composite or fiber composite materials. The application further relates to the use of the material or fuel produced according to the invention for the generation of energy from biomass.

Biomass comprises, contrary to fossil fuels, renewable raw materials which are available in the long term as domestic energy carriers, as well as all liquid and solid organic substances and products of biological and biochemical processes and their conversion products which have a sufficiently high carbon content for this method and which can also otherwise be processed in their composition and property to economically usable reaction, intermediate, secondary and end products by the method according to the invention including fuels. The feed materials are for example among carbohydrates, sugar and starches, agricultural and forestry products, also specially cultivated energy plants (fast growing tree types, reeds, whole grain plants and similar), soy, sugar cane and grain straw, as well as biogenous residual, waste substances and secondary products, plants and plant residues of different origin (grass verges, landscape cultivation goods and similar), agricultural waste including straw, sugar cane leaves, waste grain, unsalable parts of agricultural products as for example potatoes or sugar beets, decomposed silage parts and other fodder leftovers, grass clippings, grain straw, beet leaf, sugar cane leaves, carbon-containing residue and waste materials including organic waste, high-heating value fractions of house and industrial waste (residual waste), sludge, different types and classes of wood including forest wood, timber, pallets, old furniture, saw dust, residues and waste from the food industry including kitchen and food waste, waste vegetables, waste grease and paper and pulp, textiles in particular of natural fibers and natural polymers and animal excrements including liquid manure, horse manure and poultry droppings. Cadavers and in particular animal cadavers can also be counted among biomass.

As treatment of the feed material and/or of the solid-fluid mixture in the sense of the application are to be understood all influences or effects on the solid-fluid mixture which serve for the conversion of the solid-fluid mixture into the reaction products, in particular the supply of energy for the start-up and maintenance of the conversion reaction, including the treatment of the solid-fluid mixture at a temperature of over 100°C. and a pressure of over 5 bar.

The processing of the biomass and/or of the solid-fluid mixture in the sense of the application is the treatment of the feed material, reaction and/or intermediate products in different steps before and after the chemical conversion process. The processing comprises all steps, processes and influences or effects on the reaction partners, including the pretreatment and/or after-treatment.

As pretreatment all influences or effects are understood which influence the solid-fluid mixture for the start-up of the conversion reaction until the end of the filling process of the reaction space and the start of the supply of energy. In particular, a preheating of the feed material and a comminution with mainly, that is, more than two thirds of the components of the reaction mixture, particle size of under 10 mm within or outside the reaction space is regarded as pretreatment.

Solid-fluid mixtures in the sense of the application are all suspensions, dispersions and other dispersive systems, including liquid-containing solids, in particular biomass. The method according to the invention finds use particularly for those solid-fluid mixtures which lead to an increase of the content of the liquid phase or to a solvent and/or to the physical or chemical change of the solid which enable an improved solid-fluid separation or changed ratios with higher solid parts during the reaction progress in a physical or chemical manner. Feed materials in this context are liquid-containing or non-liquid-containing solids which are used for the production of the solid-fluid mixture.

Reconditioning or conditioning of the reaction products and/or secondary products in the sense of the application comprises all influences or effects on the secondary and/or end products of the conversion reaction, by means of which these are brought into the desired or necessary form.

The semi-continuous or continuous method in the sense of the application is to be understood as the production of reaction, intermediate, secondary and end products on a pilot plant station and/or industrial scale, in which at least one criterion, or also two or also more of the criteria cited below are fulfilled:

• • 1. The temperature, in particular in at least one pressure vessel, reactor or plant component across at least two reaction cycles continually lies above 40 to 90° C., preferably from 60 to 70° C. and/or above the boiling temperatures of the process water at one bar absolute pressure, so that a prolonged direct manual contact with the vessel or container wall, which is directly in contact with the reaction mixture of more than one minute is only possible with auxiliary means, insulating substances or additional apparatuses.
  • 2. The pressure, in particular in at least one pressure vessel, reactor or plant component continually lies above one bar absolute pressure or the environmental pressure across at least two reaction cycles. At least two containers, at least one of these a reactor, are connected in such a manner that a transport, a pressure equalization or the storage of compressed media can be realized.
  • 3. The processing of the feed materials, solid-fluid mixtures, reaction, secondary, intermediate and/or end products or other reaction participants is carried out in more than one container or vessel within the plant.
  • 4. The entire volume of the containers or vessels in which this processing takes place and which are each integral or essential components of the plants, is at least 500 liters, whereby at least one of these containers or vessels shall be moved not only by hand but only with additional auxiliary means.
  • 5. During a reaction cycle, a pretreated carbon-containing solid-fluid mixture and/or different types of feed material, biomasses or carbon compounds are used, in particular of different composition and consistency.
  • 6. Different feed material of the solid-fluid mixtures, reaction, secondary, intermediate and/or end products and/or other reaction participants, including catalysts and/or propellant or tempering media as for example water, in particular process water and/or gas such as process/synthetic gas are supplied to or withdrawn from the reaction mixture simultaneously, in a time-delayed manner, continuously, discontinuously or in intervals. The processes under 6. take place while the temperature of the pressure vessel, reactor or other plant components is above 60 to 70° C. or above the boiling temperatures of the process water at one bar absolute pressure or while the pressure of at least one plant component lies above one bar absolute pressure.
  • 7. The reaction mixture is treated within a coherent process, in particular within one single plant.
  • 8. The feed material or the reaction mixture are set in motion before and/or during the reaction cycle by the introduction of kinetic energy, in particular by at least one stirring or mixing system or a combination of stirring or mixing systems no matter of which type, preferably with cooperation of at least one non-mechanical stirring or mixing system, whereby, when using a single system, this does not comprise a magnetic coupling with only one shaft and is at the same time also operated electrically.
  • 9. Prior and/or during the cycle, thermal energy is supplied to or discharged from the feed material, particularly using at least one tempering system or a combination of different systems or apparatuses, wherein this is preferably not a commercial oven with single systems and/or does not have a wall heat transfer by a casing vessel that can be separated with a few hand grips, which is operated electrically.
  • 10. The continuous method is particularly characterized by the characteristics contained in the description and characteristic combinations of the apparatuses and devices used for the conversion of the continuous methods. Further criteria for a continuous method can be derived from the characteristics contained therein, where carbon-containing feed materials are continually fed to a first reactor and the reaction mixture is guided from one reactor to the next in batches and reaction products are continuously discharged from a last reactor.

A container is to be understood as an object open or closed at the top having a cavity on its inside which particularly serves for the purpose to separate its content from its environment. A container in which the conversion reaction, that is the treatment of the solid-fluid mixture, and/or the processing of the solid-fluid mixture is carried out, for example a pressure vessel or a reactor is formed by a reaction space or pressure container space closed to the outside.

As a reactor is particularly described a container in which decisive reaction steps take place. As decisive reaction steps are particularly understood the steps which run to a great extent for example in a temperature and pressure region, which has to be present on average to be able to convert at least 10 to 30 percent of the feed material into one of the mentioned reaction, intermediate, secondary or end product.

Reaction spaces or pressure container spaces are defined by the existence of spatial regions also within only one reaction or pressure container space, in which are present reaction conditions which are measurably deviant from one another. A deviant reaction condition thereby comes about through a constructive, mechanical condition and is dependent on flow and/or phase, chemical, electrical or electrochemical conditions or other type of influences. The apparatus used for this purpose goes beyond an autoclave for laboratory purposes equipped with an electrically operated stirring or mixing system with a single shaft with magnetic coupling and features a wall-side heat transfer of a compression-loaded smooth inner side of the outer reactor wall by an electrically heated casing container which can be separated with a few hand grips.

The reaction cycle, cycle or reaction is to be understood as the duration of a single conversion reaction which starts with the introduction of the starting products into the reaction space and the supply of energy which serves for the start-up of the conversion reaction. A cycle lasts from the start of the reaction process to the existence of the desired reaction product in the reaction mixture without after-treatment or conditioning, or until the completion of the reaction process.

Apparatuses which transfer the energy to the reaction mixture mechanically or by means of ultrasound, depending on flow, thermal conditions or depending on construction and thereby effect a movement of the reactor content by stirring or agitation are among the stirring or mixing systems. The movement of the reaction mixture by apparatuses such as pumps, liquid stream mixers or jet vacuum pumps, spray valves or jet nozzles and mechanical and thermal mixers or the direction of the reaction mixture along pressure gradients are also among these.

A plant consists of at least two apparatuses or devices for carrying out the method according to application. At least two containers or vessels, at least one of these a reactor, can be connected in such a manner that a pressure equalization or the storage of compressed media can be realized. An integral or essential component of the plant is an apparatus or a container when, in the case of a failure of this component, the efficiency of the method is restricted in particular in view of its cost-effectiveness by at least two, or by five, and by at least ten percent.

A coherent process is present if apparatuses or devices of a plant are commonly used. More than 200 kilograms of feed material can be processed in such a plant per week in relation to the dry matter. A plant is commonly used when apparatuses or devices are connected to one another or by line connections or spatially by methods which allow an exchange of starting, intermediate, secondary and reaction products and also other reaction participants or the common use of the same within a radius of 50 km.

The start or the initiation of the reaction or of the reaction process is characterized by the achievement of at least one target parameter of the reaction procedure including pressure or temperature, where the conversion reaction of the hydrothermal carbonization can take place over a period of at least one hour. The end of the reaction process is characterized by the continual leaving of at least one of the target parameters of the reaction procedure prior to the emptying of the reaction space. Reaction, intermediate or secondary products or partners in the sense of the application are all solid, liquid and gaseous substances which are or have been under operation conditions (pressure higher than 5 bar, temperature higher than 100° C.) independently of their length of stay in the reaction space.

Solid-fluid-mixtures in the sense of the application are all suspensions, dispersions and other disperse systems, including liquid-containing solids, in particular biomass. The device according to the invention is in particular used for those solid-fluid mixtures which lead, during the reaction process, to an increase of the content of the liquid phase or to solvent and/or to the physical or chemical change of the solid which enable an improved solid-fluid separation or changed ratios with higher solid parts.

Suspensions and dispersions are both heterogeneous solid-fluid mixtures. A heterogeneous (immiscible) substance mixture of a liquid and a solid is to be understood as a suspension. A suspension has at least one solid phase and at least one liquid phase. Colloidal dispersions, micelles, vesicles, emulsions, gels and aerosols as for example paints, emulsions or foams are among the disperse systems, that is binary mixtures of small particles and a continual dispersion medium.

Maillard-like reaction products in the sense of the application are to be understood as compounds which are intermediate, secondary, end products or reaction partners of Maillard reaction products and which can possess similar chemical, physical or biological properties. The advanced glycation end products (AGE) which are generated by rearrangement of the primary Amadori products are among these compounds and which further react to the end products of the Maillard reaction, the advanced glycation end products (AGE). The AGEs can form crosslinks with other proteins through rearrangement and polymerization. Due to the development path, there are numerous different and complex forms of AGEs, whereby NE-(carboxymethyl)lysine (CML), furosine and pentosidine have been examined most intensely up to now.

Polytetrafluoroethylene (PTFE)-like substances are to be understood as substances and compounds of similar or related or non-related classes having at least one or several characteristics of polytetrafluoroethylene as for example reaction inertness, very low friction coefficient, very low refractive index, high heat resistance, low adhesion durability of surface contaminations or smooth surface.

Fuels are substances which serve for the energy production and which are converted into energy by means of chemical, electrical or other methods. Materials are substances which are processed into a product by further processing, treatment or conditioning or which go into an end product as work objects.

The characteristics of the reaction product such as degree of purity, form, structure, density, mechanical resistance or strength, particle size, surface structure, composition, combustion characteristics, fuel value and energy content depend on the methods or reaction conditions, that is, the parameters which are responsible for the control of the method according to the invention, that is, for the process procedure.

The feed material and the reaction, intermediate, secondary and/or end products are processed in different steps before and after the chemical conversion process. The processing steps aim for a substance conversion in the industrial or technical measure. Thus, processing is to be understood as more than a manual disassembly or a manual comminution with a pair of scissors. The processing of the biomass and/or the reconditioning of the reaction products and/or the secondary products in the method according to the invention goes beyond an electrically operated stirring or mixing system with a single shaft with magnetic coupling and features a wall-side heat transfer of a compression-loaded smooth inner side of the outer reactor wall by an electrically heated casing container which can be separated with a few hand grips. It also comprises the criteria mentioned for the stirring or mixing system and/or tempering system mentioned under point 9 and 10 for the semi-continuous or continuous method.

The biomass can usually already be comminuted before the storage, and particularly before the actual conversion process, in particular before and/or after the filling into the reaction space. An apparatus for milling, for example a grinder or a wet mill is usually used for grinding. Different chaffing, mill, and or wet mill types are used depending on the feed material and the desired particle size. The particle size influences the reaction progress. Thus, the smaller the particle size, the larger is the surface of the feed material. The larger the surface of the reaction partners, the faster is the chemical conversion. The particle size of the comminuted biomass can thus be under 10 cm, also under 1 cm, and also under 2 mm.

The energy, time and material effort during the comminution process is thereby dependent on the process procedure and in particular on the configuration of the feed material, particle size and length of stay.

The incubation in an acid environment or medium with a pH-value which is below 6, also below 5, and also below 4, below 3 or also under 2, is part of the pretreatment. The necessary time of this step decreases with increasing comminution and with decreasing pH-value. The incubation at an acidic pH-value can for example take place after the comminution.

The incubation takes place in an insulated incubation vessel equipped with a double wall or another tempering system. The tempering system is essentially used via process heat or waste heat from the production process according to the invention or another process or with partially purified and heated process water. The incubation period is at least 10 to 60 minutes, 1 to 10 or 10 to 60 hours. A preincubation can considerably reduce the reaction time in dependence on the feed materials and other pretreatment steps. The savings in time are over 3-10, 10-20 percent or more under ideal conditions.

As water is produced chemically during the conversion reaction and is split from the feed materials, the water volume increases with the progression of the proceedings. The necessary reaction volume for the reaction space for example necessary in the following reaction vessels is reduced by the withdrawal of water. Thus, the volume of each individual reactor reduces in the sense of a reactor cascade during the course of the reaction. Process water can be obtained during or after concluding the conversion reaction. The withdrawal of process water during the process takes place at a temperature of above 180° C. and a pressure of over 5 bar. This makes special demands of the apparatuses and methods for the solid-fluid separation. Several sieving processes (coarse sieving, fine sieving), filtration processes and/or the centrifugal force deposition by cyclone, dynamic, static, vacuum, pressure and sterile filtration, among these especially cross flow filtration including micro, ultra, nano filtration and reverse osmosis methods are among the last-mentioned methods. Preferably, apparatuses are used where the method or functional principle taken as a basis of hydrocyclones, centrifuges, separation devices supported by force fields and/or filtration methods is used. The preferred filtration methods are especially those which can also be used with the reaction conditions of the hydrothermal carbonization. Rotation disk filters or centrifugal membrane filters are preferably used for the solid-fluid separations.

Different methods of the solid-fluid separation can be combined with one another. Each reactor following the first reactor can be connected to an apparatus for the solid-fluid separation. The solid-fluid separation takes place continuously or intermittently over a period of at least one twentieth of the dwelling time in a reactor. It can be adapted to the requirements depending on the needs and performance of the apparatus used. The withdrawn process water is kept in an insulated corrosion-resistant vessel or pressure vessel under air exclusion.

For enriching the process water, it is either removed directly from the running process from a reservoir for untreated process water. The enrichment of process water is carried out on the one hand by one or several apparatuses for the solid-fluid separation mentioned in this patent specification and/or on the other hand by evaporating water for example in an evaporator. The water vapor obtained from the evaporation process is used at another location in the process, for example for heating the feed materials prior to entry to a heat exchanger, heating of thermal oil via a heat exchanger process or for operating an apparatus for drying of reaction products such as an air agitator mill or at another drying apparatus mentioned at another location of this document.

At least 1-5, 5-20, or 20-70 percent of the water is removed for the enrichment of the process water. For this other methods mentioned in this patent specification will also be used, as for example reverse osmosis, however, with the disadvantage that the temperature has to be reduced more due to temperature-sensitive membranes. The process water is stored in an insulated and corrosion-resistant vessel or as a process water reservoir designed as a pressure vessel if possible with exclusion of air.

Enriched process water is partially used for the preincubation, preheating of feed materials, production of a pumpable solid-fluid mixture, for the absorption in the reaction mixture, for coating of admixing to provided feed materials in a reactor of the plant, for returning into the running process, as heat carrier medium for further processes within or outside a plant and/or as fertilizer component. The process water is obtained at temperatures of 1 to 50° C. over the temperatures for the respective use.

For the preincubation, preheating of feed materials, production of a pumpable solid-fluid mixture or for coating of or admixing to a provided feed material in a reactor of the plant, it is advantageous to use process water or enriched process water with a temperature of 25 to 50, 50-70 or 70-99° C. The pH-value is advantageously below 6 or below 4 or below 2 for these purposes. It is advantageous to use process water or enriched process water with a temperature of 25 to 50, 50-70 or 70-99° C. as heat carrier medium for further processes within or outside a plant. Temperatures of over 100 or 200° C. can however also be of advantages for these purposes, as well as for the admixing to a provided feed material in a reactor of the plant for return to the running process.

The necessary pH-value is obtained on the one hand by the amount of evaporated water or which is eliminated in another manner, and on the other hand by the use of acid as catalysts, the boiling point of which is above the one of water. Enriched process water contains catalyst components insofar they have a boiling point above the one of water. Sulfuric acid has thus for example a boiling point of 279° C. The decomposition point of phosphoric acid is 213° C. An acidization, that is a decreasing pH-value is achieved by continuous evaporation of water at temperatures below the boiling point of the acids, even if it can hardly be avoided that catalyst components escape with the process water from the process water despite a higher boiling point. Similar is also valid for metallic catalysts such as iron (II) sulfate with a melting point or a decomposition point above 400° C., iron (III) chloride with a boiling point above 120° C. (sublimation) or iron (II) chloride with a boiling point of 1026° C. One or several catalyst components can be cut down on by the enrichment of process water.

The process water vapor is used at another location in the process, for example for heating the feed materials prior to entry into a heat exchanger, heating of thermal oil via a heat exchanger process or for operating an apparatus for drying reaction products such as an air agitator mill and/or at a drying apparatus mentioned at another location of this document. A cleaning of the process water vapor takes place depending on the application. Enriched process water can be conveyed with several pumps mentioned in this document at temperatures also above 250° C., for example by a helical displacement pump. The temperature is decreased for example via a heat exchanger at ambient pressure or prior to the feed into an apparatus or a mixer at ambient pressure, so that the soli-fluid mixture has a temperature of 50-60 or 60-80° C.

In particular metallic, inorganic or sand-like substances and other contraries are separated from the biomass. Methods and processes are used within the scope of the treatment of the biomass and organic waste which are established for example in biogas plants. A catalyst with or without addition of water and/or in an aqueous solution can be added after the pre-incubation in the acid medium.

The biomass is thoroughly mixed with the catalyst or the catalyst mixture. The catalyst then forms, together with the biomass, a reaction mixture. The mixing process alternatively takes place within a reactor. The compaction of the reaction mixture can take place in one or several steps outside or within a reactor. A high compaction is advantageous, which again means a better usage of the reaction space. The measure of the compaction depends on the transferability into a reactor, from the desired reaction product and from the process procedure. The reaction mixture can for example also be introduced into a reactor after the pretreatment. A preheating can for example occur before the introduction of reaction components into the pressure container space. All reaction partners can be preheated. Among the feed material, all, but in particular the biomass, can be heated to approximately 60-90° C. The preheating takes place for example by the supply of heat energy and in particular by addition of process water close to boiling, a preheated biomass suspension or other water at about one bar absolute pressure or by the supply of water or process steam or other heat energy carriers. Heat energy from heat exchanger processes can alternatively or additionally be used for this.

The reaction time is, depending on the desired reaction product, between one to 60 hours, between three and 40 hours or between five and 18 hours. The reaction time is considered as finished or the reaction as terminated, when no noteworthy enthalpy is released anymore. A minimal pretreatment and/or the omission of individual pretreatment steps can increase the reaction time to over 60 hours. The reaction time depends on the composition and the characteristics of the respective feed material. The larger the surface, the smaller the particle size, the smaller the lignin or cellulose proportion and the larger the carbohydrate proportion, the faster the heat energy is released in the depolymerization phase and the faster the stabilization phase is reached and the reaction or retention time is reduced. The shorter the conversion time of the respective feed material, the greater the delay can be for example the introduction into an already running reaction in the reactor. A shorter reaction time is also achieved with relative large proportions of fat and non-vegetable, non-crosslinked, for example animal or bacterial proteins. The expiration of the heat energy release during the reaction process is an indicator for the end of the conversion process.

According to the invention, temperatures of up to 300° C. can be achieved. But temperatures between 185 to 205° C. are advantageous as well as 215° C. or 225° C. According to the invention, a pressure is built up under exclusion of air, which is for example between 7 and 90 bar. A pressure between 11 and 18 bar is advantageous, also between 18 and 26 bar and also between 26 and 34 bar.

The apparatus according to the invention comprises a reactor which can be developed differently in dependence on the processes progressing therein, the used amount and the type of the solids and/or of the desired reaction product. At least one of the reactors according to the invention can for example be a cascade, tube, circuit, loop, membrane, fluidized bed and/or a stirring vessel or a stirring vessel reactor or comprise individual characteristics or a combination of different characteristics of these reactors. The fluidized bed of the reactor is preferably circulating. The reactor according to the invention or a combination of the different reactors can be used for different treatment times and processing steps within a plant. Furthermore, the reactor can be designed as a pressure vessel due to the necessary pressure. The design of the pressure vessel form depends on the process procedure and on the mixing technique used.

In a further embodiment of the object of the invention, the reactor is formed as a type of multi membrane fluidized bed reactor with a circulating fluidized bed. Such a reactor combines the advantageous characteristics of different membrane and fluidized bed reactor types.

The reactor according to the invention can have one or more of the following characteristics.

The reactor can comprise at least one pressure container and at least one apparatus for the solid-fluid separation and is then also called a membrane reactor. The reactor can have at least one coarse and/or a fine filtration or a combination of both apparatuses, which can also be combined into a filtration apparatus. At least one of the pressure vessels can have a stirring and/or mixing system, which can thereby be called stirring vessel reactor. The sum of all reaction spaces of the pressure vessels or reactors can have a volume of 0.5 to 10,000 cubic meters, also of 5 to 2,000 cubic meters, and also of 50 to 500 cubic meters.

The sum of all containers of a plant including the reaction spaces of the pressure vessels or reactors, hoppers and storage spaces can have a volume of 0.5 to 10,000 cubic meters, also 10,000 to 70,000 cubic meters, and also 50,000 to 500,000 cubic meters. Depending on the feed material and the biomass, the water content of the biomass can be up to 95 percent or more of the total weight. The integration of a dewatering process which precedes the conversion reaction can be useful for this reason. Due to the high moisture content and the low packed weight of many biomasses, the transferability is limited, so that the initial solid proportion in the reaction space can be approximately between 5 and 30 percent. The yield of the reaction product can thereby be in the region of a single figure percentage related to the total reaction space volume. As a consequence, a relatively large reaction space volume is necessary. Large reaction space volumes can be realized by connecting several pressure vessels or reactors.

By a connection of several pressure containers or reactors, for example in the sense of a cascade, and/or the combination of different reactor types, a more advantageous retention time distribution and therefore higher operational capacity can be realized through an improved control of the process progress. At the same time, the different requirements of the different reaction phases and partial steps can be accommodated. A more favorable heat exchange can for example take place in a tubular reactor, a better mixing and remixing in a stirring vessel or stirring reactor. By the breakdown of the entire volume of the reactor into several pressure vessels, the ability to transport individual plant components including the pressure vessel is improved. By the connection of several pressure vessels or reactors, the realization of a continuous or semi-continuous process is facilitated. At least one pressure vessel for the reception of the compressed process gas formed or contained in the reactors can be used and integrated into the plant. The process gas is cleaned in an own cleaning process for example in an air cleaning plant, before it is discharged to the ambient air or it is fed to the combustion air in its own combustion process within or outside the plant. The process gas is fed in the oxidation process in line with a wet oxidation, which operates with compressed air. If a heat recovery is connected with this process, an advantage results that oxidizable components in the process gas are converted to heat energy and are recovered via a heat exchanger process.

The solid portion can be increased during the method by continual separation or withdrawal of single reactants as for example water during the process progress. The solid content can increase from for example originally 15 percent to 20 to 30 percent, 31 to 45 or 46 to 70 percent, depending on the reaction procedure or treatment conditions. The volume per reactor can simultaneously decrease as the reaction progresses. At the same time, feed material which can be converted faster can be added so that a higher operational capacity at a given reactor volume can be achieved. A connection of several reactors in series which are for example separated by valves, further enables a selective filling or refilling of individual pressure vessels with fresh feed material, reactants or catalysts for the purpose of increasing the throughput. The transfer of the reaction mixture from one pressure vessel to the next essentially takes place at operating conditions in the sense of a continuous process management.

The reactor according to the invention can comprise a vertical cylindrical basic body. The diameter-height ratio is at least 1:0.5, 1:2, 1:5 or larger. The upper base can be formed as a torospherical head. In the upper part, preferably the upper half or the upper two thirds, it can comprise a conical form with a slowly growing diameter towards the bottom. The cone-shaped base can comprise an angle to the reactor axis of 45 degrees, 40 degrees or smaller than 35 degrees. The transition of for example from the wall to the base region can be rounded to minimize disruption of the flow. The placement of the nozzle for the supply of the reaction mixture can be variable and is for example in the upper half, preferably in the upper third of the pressure vessel. The supply can take place via a valve via the outlet nozzle which is approximately in the centre of the base or the cone base. The components and the nozzles of the reactor can be connected by welding. The lid can be mounted. With a preferential use of liquid stream mixers or jet vacuum pumps and full jet nozzles, the ratio of the diameter to the height can be approximately at one to two to one to three, but also at one to four to one to five, and also at one to five to one to six.

A membrane reactor is an apparatus which allows the combination of at least one chemical reaction with a membrane method or a solid-fluid separation. Thereby, both processes are coupled integrally, so that synergies can develop. Both processes can be accommodated simultaneously in a single housing or a plant. During the chemical reaction, at least one component of the reaction mixture is converted. By the use of a membrane reactor, reaction, intermediate, secondary and end products can selectively be removed from the reaction mixture, educts can be added in a controlled manner, or the contact of the educts can be intensified. Reaction, intermediate, secondary and end products, and in particular water is removed continually or in intervals from the reaction mixture. A distinct increase of the throughput can thereby be achieved.

The combination, positioning, design and control of the respective tempering system results from the process procedure and particularly depend on the composition of the feed material. All process water systems outside and within the reactor can be used for the tempering process. This can take place on the one hand by external, that is, heat exchange processes outside the reactor, and on the other hand by the introduction of tempered process water as a thinning, tempering, suction medium or propellant for mixers, pumps and/or nozzles as aspired material for the liquid jet or jet vacuum pumps. A mixing of process and fresh water can also serve for an optimized reactor tempering. The process procedure can thereby additionally be optimized, by for example decreasing the concentration of certain inorganic substances. The introduction can advantageously be a tempering medium, in particular by injecting tempered water or recycled process water at locations which are critical with regard to the temperature. The tempering is additionally controlled via the process procedure. In addition to the combination of feed material, pH-value sample preparation and catalysts, the time-delayed introduction of feed material in dependence of its conversion characteristics is an essential element of the temperature control. During the progress of the method, the viscosity, density and magnitude and other characteristics of the feed material or the reaction mixture change. These changes can be attributed to chemical reactions and structural changes of the carbon-containing feed material, which can also be attributed to the depolymerization and later to the restructuring of the feed material. Thereby, different requirements are made of the mixing process in dependence on the process procedure. A mixing and/or flow distribution which is as even and homogeneous as possible, depends on the state of the process, the feed material, the solid concentrations and the requirements which are made of the reaction product.

The materials present in the process water depend on the mixture of the feed material and the process procedure including the catalysts. Materials previously bound to the biomass are dissolved by the procedural disintegration. Numerous elements including chlorine, sulfur, nitrate and their salts and metals, in particular heavy metals and minerals and alkalis as for example potassium or sodium and their salts pass into the aqueous phase in a certain part during the chemical conversion process. One part is again bound in the solid phase. The remaining part remains in the liquid phase. The parts of the materials which go into the liquid phase, are also dependent on the concentration difference, that is, the concentration already present in the liquid phase. A saturation up to the precipitation of certain materials takes place with increasing concentrations. Inorganic materials and compounds, for example sulfate and chloride, can thus precipitate as salts and thereby influence the process procedure and the reactor components unfavorably. The part of organic carbon compounds in the liquid phase can be above 50 g per liter. The chemical oxygen demand (COD) value of the process water is already in the higher 5 digit region (mg O₂/l) without recycling and thereby significantly exceeds the legal introduction boundary values. The chemical oxygen demand (COD) is to be generally understood as the amount of oxygen that is necessary to chemically oxidize all organic contents of a defined material amount. A process water fraction of 10 to 35 percent, also from 35 to 60 percent, or also from 60 to 85 percent is recycled in dependence on the moisture content of the feed material and the process procedure including the solid-fluid ratio. An almost complete return of the process water, that is, a circuit closure or restriction of the process water circuit is only possible in a limited manner with the aim to save fresh water and to reduce the waste water volume.l In addition to the accumulation of organic carbon compounds, an enrichment of inorganic materials such as sulfate, nitrate, calcium, chlorine, phosphorous or their compounds results. Inorganic contraries concentrations accelerate the corrosion. Lime deposits disrupt the flow in the reactor and also damage mountings such as pumps, valves and nozzles. The requirements and cost of the design of the reactor increase thereby. Sulfates can precipitate. The duration of the accumulation or saturation depends on the material composition of the feed material and the process procedure.

The chemical conversion process usually lasts several hours. During this time, complex chemical processes connected with material changes take place which have to be considered for the optimization of the process procedure.

Different types of biomass are supplied in intervals in the first two to three process phases. Depending on the desired reaction product, reaction products are for example withdrawn towards the end of the last two process phases. Propellant or tempering means as for example a gas, water, in particular process water and/or process/synthesis gas and catalysts are withdrawn or supplied during the running process. Reactants and in particular secondary products are removed, which disturb the course of the chemical reaction, the mixing and also the flow.

Different methods can be used for the deposition of the solid materials and in particular the reaction products in the reaction mixture. The solid-fluid separation serves for the separation of the liquid phase, whereby a concentration of the solids is achieved. Different sifting processes (coarse sifting, fine sifting), filtration processes and/or the deposition by centrifugal force by means of a cyclone can be combined with one another for the separation of the solids. So as to reduce the effort of a filtration or the sifting during the process, one or several filtration or sifting processes are carried out within the scope of the pretreatment.

From these two methods, at least one coarse or one fine filtration or a combination of these two methods can take place. By means of the filtration methods, in particular micro and/or ultrafiltration method or a combination of both, one third to two thirds of the total organic carbon compounds can be removed from the process water. The solid-fluid separation is preferably carried out at operating conditions, and usually goes beyond the use of simple paper filter as are for example used on a laboratory scale. The choice of the used methods depends amongst others on the chemical composition, particle size distribution, density, particle form, firmness and solubility and includes the use of electrical currents and loads, different densities and centrifugal forces and different particle sizes.

The dynamic, static, vacuum, pressure and sterile filtration, amongst them in particular the cross flow filtration including available micro-, ultra-, nanofiltration and reverse osmosis method are among the apparatuses used. Preferably apparatuses are used where the underlying method or function principle of hydrocyclones, centrifuges, electrical or magnetic separation devices and/or filtration methods is used. The preferred filtration methods are particularly among those which can be used with the reaction conditions of the hydrothermal carbonization. For the solid-fluid separation, in particular at operating conditions, rotation disk filters or centrifugal membrane filters are preferably used. The preferred material which is responsible for the formation of the pores consists of metal and in particular of ceramics. The form of the pore-forming material is preferably disk-shaped. Depending on the filtration method used and materials introduced, there is not always present a proportional ratio of pore size of the filter and the solid amount in the filtrate. This particularly applies to the use of ceramic materials for the filter elements. The aqueous phase is introduced into a process water reservoir in a filtered or unfiltered manner. The characteristics of the solids to be separated, and thereby the choice of the methods chosen for the separation depend on the process procedure and on the characteristics of the desired reaction product. The further the process has progressed and the higher the density of the reaction product, the easier it is to carry out the separation process. The separation preferably takes place near the operating conditions. The solid amount in the filtrate usually sinks proportionally to the pore size and can increase significantly by the use of an ultrafiltration method and be over two thirds to four fifth. One or several apparatuses for the solid-fluid separation are integrated into the process for the elimination of sand and other contraries with a high density or a high weight which become separable in the course of the treatment of the biomass. The use of the principle of the centrifugal force separation of solids is particularly advantageous for the cleaning of the process water which is used as propellant jet medium to protect pumps, mixers and nozzles.

Process water is withdrawn for reconditioning or treatment during the process at one or several locations from the upper half the upper third or from the upper quarter of the reactor. Reconditioned or treated process water is returned to the water circuit of the plant for recycling. At least one and preferably several process water reservoirs can be used for every individual reactor or for several combined reactors. Different cleaning steps precede the individual process water reservoirs. The volume of individual or a common process water reservoir is approximately 35 to 85 percent of the total volume of all reactors in its sum. The process water reservoir is designed for the temperature and pressure load of the reactors, so that pressure reduction and heat exchange apparatuses are not compellingly necessary.

A process water cleaning is integrated into the water circuit of the described plant. Different treatment or reconditioning methods are necessary depending on the use of the reconditioned process water. Different mechanical, chemical and biological methods and apparatuses are used for this individually or in combination. Aerobic and anaerobic high performance bio reactors, bio membrane reactors, anaerobic and animate slurry methods. The above-mentioned methods and apparatuses integrated or connected into the process water circuit shall decrease the content of organic compounds in the circuit water considerably, but the measure of the return of the process water has to be made dependent on the concentrations of organic substances which are not sufficiently disintegrated and high alkali metal or mineral material concentrations as for example calcium. So as to be able to return a part of the process water as high as possible, a particularly effective combination of different methods and apparatuses is to be used.

The apparatus for the mechanical waste water cleaning is a filter, a microfilter or an ultrafilter, and can be congruent with the methods for the solid-fluid separation described above. The apparatus for the solid-fluid separation, into which the filter(s) are built, is preferably a rotation disk filter and especially a centrifugal membrane filter. For the biological cleaning of the process or waste water, an apparatus is used which soonest satisfies the complex requirements for cleaning or treatment. For example, an apparatus in the steel construction manner is to be used preferably, for example a high performance bioreactor in the biomembrane method, preferably an aerobic process water treatment, especially a loop reactor. The loop reactor should have an effective nozzle for mixing the solid and liquid phases in its design. Alternatively or additionally to the aerobic method, a reactor for the anaerobic process water treatment or also reverse electrodialysis (electrodialysis reversal) can be used, particularly for the nitrate recovery, distillation, vaporization and/or ion exchange methods and active coal.

The cooling of the reaction product, in particular below the boiling temperature at one bar absolute pressure usually takes place outside the reaction space, also in an apparatus for devolatilization. The heat energy released thereby can be made available for other processes via heat exchanger processes. One or several comminution steps take place before, during or after this process. For this mills or pressing methods are preferably used.

The separation of the solid phase from the reaction mixture usually takes place in the first step in mechanical and in the second step in thermal separation devices.

A static thickener is used for reducing the water content under the action of gravity with or without mechanical rotating apparatus or a raking machine, for example a stationary thickener or a throughput thickener. The control of the supply amount can be made by a dosing device. The device enables to dispense the thickened mixture evenly dosed and to several machines with a correspondingly high volume. The thickener can also be integrated directly into the drying apparatus. An advantageous design of the cone construction makes it possible that the drying apparatus is charged directly with the mixture. External installations can be foregone with a corresponding adjustment of the process magnitudes. The mixture to be thickened can alternatively be introduced under pressure to an arched sieve surface or a curved screen. The resulting centrifugal force presses a part of the liquid through the sieve slots. The thickened mixture is combined at the end of the sift course and fed to the drying appliance. A hydrocyclone offers a further advantageous separation method, in which solid and liquid are separated by centrifugal acceleration. The thickened mixture in the underflow is supplied to the drying apparatus and the processed or clarified liquid leaves the hydrocyclone in the overflow. A continuous and an optimized supply to the drying apparatus can be ensured by preceding and adjusted thickening devices and interposed dosing apparatuses. This is particularly important with the use of a shear centrifuge for drying. Shear centrifuges have a high operational safety and are suitable for dehumidifying and washing of granular solids.

Thermal drying methods are preferably used for drying in addition to mechanical apparatus which often has to be connected ahead of the drying for energetic reasons. The amounts supplied to the drying procedure have a weight above one kilogram. A continuous operation is preferred to a charge operation. The drying process takes place by means of at least one or several driers or by a combination of different apparatuses for separation and/or drying. A convection drier is for example used for drying the reaction and secondary products. The goods to be dried thereby come into contact with hot drying gas. It is hereby disadvantageous that the used gas has to be discharged and usually has to be cleaned with dust separators. The gas is possibly returned to the moisture after condensing. A fluidized bed drier can for example be used as convection drier. Spray, nozzle tower or flow driers can also be used depending on the present or desired particle size. A continuous process is advantageous, where one or more tray, drum or tunnel drier are used. When a contact drier is used, essentially only the contact surface is available for the heat transfer. A belt, vacuum belt, drum, screw, cylinder, roller or belt drier and preferably a vacuum drum filter or drier is used. For achieving lower moisture contents, a disk drier can alternatively or additionally be used, depending on the throughput. The drying process can take place by means of a hot gaseous medium as for example air at temperatures between 61 and 95° C., between 65 and 90° C. or between 70 and 85° C. Alternatively, overheated water vapor or water vapor having a temperature of 130 to 180° C. is used above all in the thermal drying apparatuses.

A combined mechanical-thermal method can be used for the separation or for drying. The advantage of a mechanical-thermal process compared to the conventional methods is significantly lower residual moisture of the product, whereby an improved conveyability or transportability of the product is achieved, especially with fine particle or nanosystems. It is a further advantage that a partial washout of contaminations from the reaction product takes place by means of the condensating steam. The use of steam as a further driving dehumidification potential results in an increase of the performance for centrifuges working in a filtrating manner. The mechanism of the even mechanical displacement by a condensation front cooperates with the mass force and practically leads to a complete depletion of the coarse capillary system. Steam pressure filtration is for example among the methods using this mechanism. It uses saturated or overheated steam for a gas difference pressure removal instead of pressurized air. A steam pressure superposed centrifugal dehumidification is used especially preferred. In a method space, the process of the combined steam pressure and centrifugal dehumidification transfers the fine disperse solid of the reaction product from the suspension into a dry, pure, free flowing end product according to the invention. The residual moisture content of the reaction products according to the invention is advantageously about 6 to 25 percent, also 10 to 20 percent or also 12 to 15 percent. The reaction mixture is present as a suspension after the conversion reaction. Among others, the following reaction, intermediate, secondary and/or end products result in dependence on the feed material: Fuels ranging from peat-like, over lignite-like to black coal-like fuels, humus, Maillard- or Maillard-like reaction products, carbon-containing materials such as insulating materials, nano sponges, pellets, fibers, cables, active or sorption coal, charcoal substitute material, highly compacted carbon products and materials and in particular also feed material for graphite and graphite-containing or -like products and carbon fibers and feed material for composite or fiber composite materials.

Pure, purest and ultra pure coal-like materials belong to the products according to the application. They have advantageous characteristics, which can mainly be ascribed to the reduction of mineral materials compared to the feed material. Pure coal is mainly to be understood the combustible part of the coal and purest coal is also to be understood as active coal or charcoal. The mineral content of ultra pure coal is for example under 0.1 percent by weight.

Organic and also inorganic materials are also removed from the feed material during the course of the method or the chemical conversion process and are thus made available and more easily accessible. The improved accessibility is in part due to the dissolution of previously inaccessible or chemically bound materials that have partially gone into the aqueous phase. The degree to which this occurs depends on the reaction or treatment conditions. In addition to the organic dissolved and non-dissolved materials, inorganic materials such alkalis, metals, salts and acids including humic acid-like materials, calcium, magnesium, chlorine, iron, aluminum, phosphorous, potassium, sodium, nitrogen and their compounds are also among the materials which are removed or available and more easily accessible.

The solid carbonaceous components of the reaction product, which are present as materials and/or fuels after the conversion reaction, have the following characteristics amongst others: The composition of the materials and/or fuels can be controlled by the reaction procedure. The concentration of individual materials cannot readily be varied selectively and independently of other materials offhand. However, different material groups and parameters can be changed in the same direction. For example, during a reduction of the sulfur content, the chlorine and ash content is also reduced at the same time.

In different measurements by means of elemental analysis, the carbon fraction for grass, cut hedges (thuja) and sugar beet was over 50 to 63 percent of the percentage mass fraction of the elements (dry mass) and was thereby approximately 20 to 60 percent above the mass fraction of the feed material. The oxygen fraction was reduced up to half, and the nitrogen fraction about a quarter, and the hydrogen fraction was reduced up to about a quarter. The carbon fraction of the materials and/or fuels is increased by 10 to 300 percent, also 50 to 300 percent, also 100 to 300 percent or also by 200 to 300 percent, compared to the biomass. The carbon fraction of the materials and/or fuels is increased by 5 to 200 percent, preferably 10 to 150 percent, 10 to 120 percent or by 50 to 100 percent, compared to the feed material. The carbon fraction of the materials and/or fuel is usually between 40 to 95 percent, also 50 to 90 percent, or also 55 to 80 percent. The carbon fraction can, in dependence on the reaction procedure and on the feed material, also achieve higher purity degrees of over 98 percent. The hydrogen fraction of the material and/or fuel is reduced up to nine tenth to a third, also a third to a twentieth or up to a twentieth to a fiftieth compared to the feed material. The oxygen fraction of the material and/or fuel is reduced up to nine tenth to a third, also a third to a twentieth or up to a twentieth to a hundredth compared to the feed material.

The nitrogen fraction of the material and/or fuel is reduced up to nine tenth to a third, also a third to a twentieth or up to a twentieth to a hundredth compared to the feed material. The sulfur fraction of the material and/or fuel can be a fraction of the biomass and is reduced up to nine tenth to a third, also a third to a fiftieth or also up to a fiftieth to a thousandth compared to the feed material. The ash fraction of the material and/or fuel can be a fraction of the biomass and is reduced up to nine tenth to a third, also a third to a fiftieth or also up to a fiftieth to a thousandth compared to the feed material. The fine dust fraction of the material and/or fuel can be a fraction of the biomass and is reduced up to nine tenth to a third, also a third to a fiftieth or also up to a fiftieth to a thousandth compared to the feed material.

A reduction of the mineral parts and of the ash and particulate fine dust part during the combustion to a multiple of for example considerably above 300 percent can be enabled by a high fraction of process water. A thinning of the mentioned fractions of substances, but also of numerous other materials occurs by the increase of the proportion of process water, which were originally contained in the feed material and which are removed during the conversion reaction and are dissolved. It could be said that these materials are washed out, so that the fraction of the soluble materials can practically be reduced proportional to the supplied process water in the solid phase. Even when a catalyst component is left out or sub-optimal reaction conditions prevail, a higher carbon fraction can still be achieved, which is more than 5 to 10 percent over the one of the feed material. A carbon fraction of 55 to 77 percent can be obtained with an appropriate treatment of the biomass and the process procedure. With an appropriate process procedure, favorable feed material, including adjustment of the catalyst mixture, carbon values of 78 percent and more can also be achieved. These values can thereby be compared to that of fossil fuels.

After the end of the conversion reaction, the carbon fraction of the material or and/or fuel has indeed increased, but the energy content or the fuel value can have decreased up to 36 percent. For heat is released during the reaction, as it is an exothermal reaction. In the reverse, altogether at least 65 percent of the original fuel value of the dry biomass is kept related to the mass weight of the feed material If carbohydrate-containing biomass such as grain, sweet corn or sugar is used as feed material, the fuel value of the material and/or of the fuel is about 65 to 85 percent, or, in another example of the embodiment, 70 to 80 percent, compared to the feed material. The less carbohydrate is contained in the feed material, the lower is the energy release during the conversion reaction. This involves a higher fuel value of the reaction product at the same time, compared to the feed material. The energy contents of the reaction product depending on the biomass used can be described as follows in an exemplary manner: If lignocellulosic biomass such as cut greens or harvest waste is used as feed material, the fuel value of the material and/or of the fuel is about 70 to 90 percent, and also 75 to 85 percent related to the mass weight of the feed material. If biomass with a low carbohydrate, cellulose or lignin fraction as for example clearing or sewage sludge is used as feed material, the fuel value of the material and/or of the fuel is about 80 to 95 percent, and also 85 to 90 percent related to the mass weight of the feed material. Pure, purest or ultra pure coal can be used in a versatile manner, for example as chemical basic and feed material for further processing in the chemical industry or as fuel for a carbon fuel cell.

Numerous materials were dissolved from the solid phase during the reaction procedure and have gone into the aqueous phase and are now present in the process water. Several minerals such as phosphorous, sulfur, but also nitrate can be recovered from the process water. These can then be used as fertilizer, raw materials or materials for other processes. In order to ensure a natural cycle it is of interest that mineral components can be isolated particularly from the liquid phase so that these can again be returned to surfaces for the natural development of biomass. An approximately closed cycle can thereby be maintained, by returning nutrients which were contained in this biomass to the surfaces from which biomass was previously extracted for the production process.

Completely new chemical carbon compounds and structures form by depolymerization and new polymerization processes. In particular, agglomerates form which can be comminuted with a lower energy input than most known solid fossil fuels. Further, a brownish or blackish coloration results in dependence on the feed material, probably by formation of Maillard reaction products. The density of many feed materials lower than water prior to the start of the reaction. The density continually increases during the reaction procedure and reaches a density comparable to black coal in dependence on the feed material and the reaction procedure. While the density of most feed material is at 200 to 600 kg/m³, and occasionally to 800 kg/m³ (dry weight), the density of the reaction product can reach above 900 to 1200 kg/m³, occasionally also values of 1250 to 1350 kg/m³, under the assumption that the air between the particles of the reaction products is eliminated or pressed out. By virtue of the small particle size of the reaction product, a larger surface results compared to the feed material. This makes the drying with the same moisture content easier than with naturally occurring carbon compounds with a comparable carbon content. The large surface contributes at the same time to a lower ignition temperature.

The differential characteristics of the reaction products are

• • the presence of Maillard or Maillard-like reaction products and the liquid and solid phase.
  • The strong and intensive odor formation varies with the feed material. The odor formation is basically connected to the formation of Maillard reaction products.
  • Improved electrical conductivity compared to other naturally occurring
  • carbon compounds with a comparable carbon content.
  • Turf- to black coal-like fuel.
  • Less volatile components than conventional or fossil fuels with the same carbon fraction.
  • Lower ash formation by combustion, lower content of nitrogen,
  • sulfur, nitrate, heavy metals and reactive, that is, lower self-ignition temperatures than with comparable fossil fuels with a similarly high carbon fraction.
  • Advantageous and less damaging composition of the flue gases by combustion than comparable fossil fuel having a similarly high carbon fraction.

Altogether, numerous advantages result from the above-mentioned characteristics of the new reaction product and its environmentally and climate friendly characteristics compared to conventional fuels. The treatment method is more efficient and economical for the purpose of an industrial production of materials and/or fuels from biomass compared to the conventional methods for energy recovery from biomass. With the material conversion of the biomass, practically no carbon has to be lost. Usually more than 95 percent of the carbon contained in the feed material passes into the solid components of the reaction product, which can be used for energy recovery. The remainder of the carbon compounds goes into the liquid phase. During the conversion reaction in the reactor, practically hardly any noteworthy amounts of carbon dioxide or other greenhouse gases are released. About 1-4 percent of the carbon of the feed material can go into the liquid phase. The fraction thereby depends on the process procedure, in particular on the carbon content of the feed material and on the liquid-solid ratio of the reaction mixture.

Carbon-containing nanomaterials and structures are formed by the reaction procedure, in particular by the choice and composition of the feed material and catalysts. These materials partially have useful material and surface characteristics. Among these are for example nano-sponges which can be used as water reservoirs or insulating materials. The so-called Maillard reaction during with heating processes such as baking, frying, roasting, grilling and deep-frying of proteins or albuminous and carbohydrate-rich food at temperatures over 130° C. During the course of the so-called Maillard reaction, red to yellow-brown, sometimes black-colored polymers, the melanoidines, result from carbohydrates and amino acids in addition to a plurality of flavoring agents. Particularly many and dark melanoidines are formed by high temperatures as they occur during baking and roasting, but the reaction is also accelerated by higher pressures. They thereby form a substantial part of the food in products such as bread, coffee, malt, nuts or cornflakes and makes for example up to 30 percent of coffee.

Maillard or Maillard-like reaction products are formed in high concentrations during the hydrothermal carbonization. In the solid (amongst others solid) and in the liquid phase (e.g. process water), there are relatively high concentrations of the indicator substance CML, which are usually between 0.3-2 mmol/mol lysine. Higher concentrations are usually present in the liquid phase, that is, in the process water, than in the solid phase of the reaction product. The concentrations or concentration ratios depend on the solid-fluid ratio and on the composition of the feed material and the process procedure. Antioxidant and chemo-preventive characteristics are assigned to CML. It is therefore to be assumed that comparable or similar characteristics can also be found with other intermediate, secondary or reaction products of the hydrothermal carbonization, including the Maillard or Maillard-like reaction products. Insulation and cleaning of the Maillard or Maillard-like reaction products take place amongst others by means of filtration, ultrafiltration and/or chromatographic methods, in particular by means column chromatography.

The humus which is produced in the method according to the invention by means of hydrothermal carbonization, results by a comparably shorter dwelling time compared to reaction products having a higher fuel value. It usually still comprises fiber-containing material (amongst others lignin and cellulose) of the feed material. The biopolymers are not completely depolymerized. The humus produced according to the invention has a carbon fraction of at least 30 to 45 percent and a heating value of at least 15 to 24 MJ/kg, and can be burnt well. The humus produced according to the method of the application can partially have similar characteristics as natural humus and partially also turf or peat.

The above characteristics for the reaction products of the method of the application are valid for the combustion characteristics. Certain materials can be enriched in the humus by an optimized process procedure, in particular by the concentration difference between the solid and liquid phase within the reaction mixture. This is desired during the utilization of the humus as CO₂/carbon sink or fertilizer. Unlike this, during the processing of admixture of humus produced according to the invention to products, where an enrichment of certain materials is not desired. In addition, an enrichment of mineral materials and alkalis and other substances, which are detrimental for the product utilization, is avoided. The humus produced according to the invention is a uniform humus and fuel, the characteristics of which can be calculated and controlled via the composition of the feed material and the catalysts, as well as the process procedure. Humus produced according to the invention can be produced within hours. The method according to the invention is thereby considerably faster than other known production methods of humus, which usually take weeks or months.

The materials and/or fuels produced according to the method of the application including turf or peat or turf-like or peat-like materials have the following characteristics:

• • By the use of the method according to the invention, turf- to black coal-like fuel results from biomass.
  • The fuel value depends on the process procedure, in particular the reaction duration. The fuel value increases with the reaction duration or the dwelling time in the reactor.
  • Less volatile components than conventional or fossil fuels with the same carbon fraction.
  • The energy yield up to coal is 0.7-0.95. The lower the carbohydrate content, the higher the energy yield.
  • 90-95%: lignins or bacterial biomass.
  • The fuels are more reactive and have lower self-ignition temperatures than comparable fossil fuel with a comparable carbon fraction of the total amount.
  • Fossil fuels such as lignite or black coal have indeed similar heating values compared to fuels which are produced by means of the method according to the invention, but they are distinctly different to fuels with regard to the composition and characteristics.

The different types and species of fossil coal have very different chemical compositions and characteristics, depending on the point of origin and mining area, so that every type of coal has unique and unmistakable characteristic features. The heating value of fossil Lausitz raw brown coal is for example 8.700 kJ/kg, the water content about 56 percent, sulfur content about 0.7 percent, and the ash content about 4.5 percent. The water, sulfur, and ash content of the fuel or material according to the invention are all lower, while the fuel value usually is clearly above 20.000 kJ/kg. One kilowatt of fossil Lausitz raw lignite can be generated independently of the water content. In contrast, more than double the amount of current can be generated from the same amount of fuel.

In the material and/or fuel according to the invention are strong verifiable concentrations of Maillard reaction products compared to fossil coal. NE-(carboxymethyl) lysine (CML) has established itself as indicator. This compound is detectable in the liquid and also in the solid phase of the reaction products. Concentrations of 0.2 to over 1.5 mmol/mol lysine were measured, whereby higher parts were measured in the liquid phase than in the solid phase. The distribution of the concentrations depends on the feed material, the reaction conditions, and the process procedure. After mining, fossil coal is present in clumps or, depending on the mining depth, in relatively highly compressed agglomerates, which have to be comminuted with a high energy effort. Further, it has to be dried and milled to a fine lignite or coal dust in coal mills. Compared to this, materials and/or fuels after the end of the process are present as small particles with a size of usually less than 1 millimeter to less than 30 nanometer and can be dried more easily due to their large surface. With this, the energy effort for conditioning and in particular drying of fuels is considerably lower compared to solid fossil coal.

The combustion characteristics of the fuel are in particular more advantageous, not only compared to fossil types of coal, but also compared to most of the currently available fuels of renewable raw materials. At least one, but often several or all of the following parameters are more favorable with fuels, in particular compared to the feed material or alternative fossil or biomass fuels: reduced ash parts, less chlorine, nitrate, sulfur, heavy metals and lower emissions of dust, fine dust and gaseous toxic substances including nitrogen and sulfur oxides. This is also valid for the compacted forms of fuels such as briquettes and pellets.

The quality of the fuel and the combustion characteristics depends on

• • the feed material or the mixture of the feed material, on the process procedure, on the catalyst mixture and on the composition of the process water.
  • Feed materials with high parts of fat and energy content lead to
  • fuels with higher heating values. For example, during the processing of particularly suitable sludges, heating values of up to 34-36 MJ/kg can be achieved.
  • The ash content after the combustion of the fuel with a fuel value of 30-33 MJ/kg is reduced by up to 75 percent and more compared to the feed material with a fuel value of 17-20 MJ/kg.
  • The sulfur content following combustion of the fuel with a fuel value of 30-33 MJ/kg is reduced by up to 50 percent and more compared to the feed material with a fuel value of 17-20 MJ/kg.
  • The fine particulate matter and gas emissions are lower compared to the feed material.
  • The combustion result is determined by the entirety of all parameters linked to the process procedure, conditioning-dependent fuel quality and combustion technique.
  • The fuel is a fuel with relatively uniform properties, the characteristics of which can be calculated and controlled via the composition of the feed material and the catalysts, as well as the process procedure.
  • In addition to the differences in the combustion characteristics already mentioned, these are additional differential characteristics to fossil fuels such as black coal, lignite or peat.
  • Pure, purest and ultra pure-like materials also belong to the products according to the invention. They have advantageous characteristics, which can mainly be ascribed to the reduction of mineral materials compared to the feed material. Pure coal is mainly to be understood as the combustible fraction of the coal, and purest coal is also to be understood as active coal. The mineral content of ultra pure coal is for example under 0.1 weight percent.

Depending on the embodiment of an apparatus according to the invention, different process steps can be combined in one unit. The comminution and mixing can for example proceed in a single mill or the drying and comminution can take place in an air turbulence mill. All apparatuses or devices mentioned in this patent specification are provided or equipped with a control, regulation, extensive automatization, as far as this is sensible in a process-technical manner, can be depicted economically and is technically possible. The same is valid for all mentioned procedures, method or process steps.

Double-stranded hydrolysis or reactor batch feeding for HTC and TDH: The invention is explained in more detail in an exemplary manner in the following by means of the drawings described in the following.

SHORT DESCRIPTION OF THE DRAWINGS

FIG. 1 shows a schematic depiction of a plant in an exemplary manner while considering a double-strand feed apparatus.

FIG. 2 shows a schematic depiction of reactors arranged in parallel with respectively a reactor connected downstream in an exemplary manner.

FIG. 3 shows a schematic depiction of a plant for the thermally induced hydrolysis in an exemplary manner.

FIG. 1 shows a schematic depiction of a plant in an exemplary manner with special consideration of a double-stranded batch feeding apparatus for the method according to the invention. The apparatus consists of the feed strands I and II, and the devolatilization strand III. The strand I serves for feeding feed materials with a high solid content of for example 3 to 50 percent related to the total volume. For this, the “dry” biomass is stored in a hopper (1) and brought to a vessel (2), preferably a bottom plate outfeed vessel (2), from there. The feed materials are fed to a comminution apparatus (3), for example executed as a wet or dry mill or as another suitable mechanical comminution unit via a conveying device, which can for example be a screw conveyor or a conveyor belt, and are fed from there into a mixing vessel (6). The dry biomass is mixed thoroughly with concentrated process water from the reservoir (4) and at least one catalyst from the vessel (5) in the mixing vessel (6) by means of an agitator. The mixture is fed to the incubation vessel (8) via the conveying device (7). The incubation vessel (8) enables a residence time of the catalyst on the material. The vessels (6) and (8) are double-walled and have a hot water connection, so as to enable a preheating of the material to 50-60° C. The incubated material of the “dry” feed materials is fed via the conveyor devices (9) and (10), which are for example designed as screw conveyors or as conveyor belts, via a feed apparatus (21) from the first feed strand to the first reactor (19) under pressure above the vapor pressure of the process water. The feed apparatus consists of a force conveyor, which is for example an injector, double screw extruder, an eccentric spiral pump, a piston pump, a spiral displacement pump, which are respectively equipped with or without compressor screws, or a double screw compressor. The feed apparatus (21) can additionally be provided with a shutoff device. The feed apparatus (21) ensures that the incubated material from the strand I with a pressure level above the inner reactor pressure is brought into the reactor (19), and prevents backlashes into the feed device.

Pumpable feed materials with a solid content of 3 to 50 percent related to the entire volume are transferred to a mixing device (14) from a storage vessel (12) by means of a conveying device (13) and mixed in the mixing vessel (14) with process water from the reservoir (4) and catalyst from a vessel (15), incubated in an incubation vessel (16) and fed to the reactor (19) via a suitable conveyor device (17), which can for example be designed as a piston, spiral displacement, or eccentric spiral pump. The material is heated to at least 160-180, 200-220 or 220 to 250° C. via the heat exchanger unit (18). The feed materials pretreated in such a manner from the feed strand II are guided from the feed strand I via the feed materials fed or presented to the conveyor previously, in a parallel manner or afterwards. The ratio of the mass flow rate of feed strand Ito feed strand II or of presented to fed feed materials is for example 1:20, 1:5, 1:1, or 10:1. An even mixture of the presented or of the fed material takes place in the first reactor via a mixing or stirring apparatus (20). The heating and the discharge of an exothermic reaction occurring with the reaction takes place via a heat exchanger apparatus (22) in connection with the double wall (23) of the reactor (19) and/or other heat exchangers brought into the reactor or which are in connection with the reaction mixture. These can for example be formed as spiral, tubular, bundle or spiral heat exchangers. After the necessary dwelling time, the content of the reactor (19) is transferred to a second reactor (24) using a drop of pressure.

A conveyor means for accelerating fluids can be used additionally. The second reactor (24) situated in the flow direction behind the first reactor (19) has a smaller volume. Because process water is withdrawn by means of an apparatus described in another part, whereby the volume of the reaction mixture is reduced. Lower reactor volumes or smaller reaction spaces are thereby needed in the further course of the process. The withdrawal of process water simultaneously also enables the merging of the diminished reaction volumes from different parallel reactors or of reaction mixtures, which are merged in a single reactor in a parallel or time-delayed manner with a reaction stage deviating up to 50 percent of the total reaction time or with a reaction time deviating up to 50 percent. The volume of this reactor is for example 5, 10 or 20 percent below the volume of the sum of all reactor volumes, from which the reactor receives the reaction mixture.

The reactor (24) is also equipped with heat exchanger device (22), a stirring device (20) and a double wall (23), and keeps the temperature over the dwelling time constant at the level necessary for the reaction. The released reaction heat is discharged via the heat exchanger device (22), whereby a cooling is achieved. After the expiration of the dwelling time for the reactor (24), a devolatilization of the material in the devolatilization vessel (26) takes place via the heat exchanger unit (25).The material can also be treated thermally via stirring device (20), heat exchanger device (22) and double wall (23). The heat exchanger (27) ensures a cooling of the material to temperatures below the evaporation temperature of water. The flow and the pressure devolatilization are thereby controlled thereby via a devolatilization pump which is directed backwards, which is formed as a force conveyor, eccentric spiral displacement or piston membrane pump.

The wet feed material is stored in the devolatilization vessel (29). Accumulated heat can be discharged via its double wall. Excess process water is separated via the subsequent solid-fluid separation (30), which is designed as a decanter, centrifuge, cyclone, filter chamber press, filtration apparatus or an apparatus for a separation or drying serving for the same purpose or mentioned in another part of this specification, and the process water is again made available for other processes within the method according to the invention. The final product is stored temporarily in the store (31) for the further use.

The feeding of a first or several first reactors can also take place via a single feed strand, that is, via the feed strand I or II alone or independent of a second feed strand. This is unproblematic, if “wet” feed materials are fed. But if a reactor is filled with “dry” and free flowing feed material, a sufficient supply of water has to be considered. The use of process water or enriched process water at temperatures of over 60, 100, 160 or 200° C. is thereby advantageous, where a filling just, that is up to 5, 10, 40 or 60 percent below the free flowing pile or of the filling level of the “dry” feed material is sufficient. The filling height with process water within the reactor depends amongst others on the bulk density and other consistency of the feed material.

So as to increase the throughput of the feed materials or the yield of the fuel or material according to the invention, an adjustment of a solid content as high as possible is necessary. The limiting factor for maximizing the solid content is the pumpability for the predominantly wet biomass on the one hand, and the conveyability independent of a pump of a dry biomass connected with the introduction a the reactor on the other hand. At the same time, it has to be considered that a preincubation also has to be carried out for dry biomass. A use of the feed materials with a particle size as small as possible as described in another part of this specification is thereby usually sufficient. The decrease of the viscosity in the course of the charging method can be seen as measure of the progression of the pretreatment. The viscosity of the solid-fluid mixture decreases when progressing through the charging apparatus and is reduced to over three quarters, to over the half or to over a fifth of the viscosity of the feed material at the end of the process. However, it is valid for the viscosity measurement, that no water was withdrawn or evaporated during the conversion process, that is, between the measurements.

FIG. 2 shows a schematic depiction of reactor arranged in parallel (19) and (24) with a respective reactor (32) and (33) connected downstream in an exemplary manner. The elements of the plants otherwise coincide with FIG. 1 and are thus designated with the same reference numerals. Reactors (19, 24 or 32, 22) are meant to be a reactor configuration, where several reactors are filled or emptied in parallel, so that a continuous inlet and outlet flow is realized. An inlet and outlet flow is continuous if at least 10-30, 30-60 or 60-90 percent of the reaction time are flown through the devices connected upstream or downstream of the at least one reactor. Heat exchangers for heating and cooling the reaction mixture are among these devices.

By means of a parallel arrangement, it is enabled that each reactor can be filled or emptied independently from another one. While a first reactor is filled and a second reactor is emptied, the reaction volume will be held in a third reactor under operating conditions for a period of 10-100, 100-300 or 300-1600 minutes. If a first reactor is filled, it becomes a third reactor, that is, it takes on the function of a third reactor, in that a dwelling time of at least 1-9, 10-30, 30-60 or 60-99 percent of the reaction time is enabled. If a second reactor is emptied, it becomes a first reactor, that is, it takes on the function of a first reactor which is filled again. A third reactor can also consist of an indefinite number of reactors.

Due to the energetic use of biogenic residual materials and agricultural products and the sanitation conditions, a thermal pretreatment of biomass gains increasing importance. By the hydrolysis and especially the so-called thermal pressure hydrolysis, which is connected upstream of a fermentation or other methods for energy production of biomass, a better disintegration especially of lignocellulose-containing biomass such as wood, grass and lopping is achieved, so that these are accessible in a simpler manner for the micro organisms and the fuel production. Highly infectious material is further sanitized and thereby gives an economic and safe alternative for example for animal meal production. By the use of this hydrolysis method, animal meal that would possibly be difficult and more expensive to produce, does not occur.

The treatment of organic wastes by fermentation leads to a reduction of the biomass use by 10 to 20 or 20 to 30 or more percent related to organic solid content for producing the same amount of energy according to the invention of the hydrolysis method according to the invention. Different method for pretreating of biomasses prior to introduction into a fermenter of a biogas plant were suggested. Among these, a so-called thermal pressure hydrolysis was developed a few years ago, where the feed materials are guided through a loop reactor (DE19723519) or hydrolysis reactor (DE3928815) and are heated to a temperature of 180° C. The execution of a microbiological hydrolysis was suggested in a tubular reactor (DE4403391). With the so-called thermal pressure analysis or thermally induced hydrolysis, biomass is treated over a period of about 20 minutes. This is a clearly lower period compared to the hydrothermal carbonization.

In the last few years, several plants were constructed for the thermal pressure hydrolysis at 180° C. Despite expected high efficiency yields, a wide use failed to appear in practice. Several pilot plants have been unable to achieve the desired solid contents continuously, as caking and blockages always resulted in the heat exchanger formed as tubular reactor. These problems lasting for years could only be avoided by reducing the solid content, which reduced the yield of hydrolyzed or heated material so that an economic usability of this technology could practically not be achieved.

The sedimentation behavior of biomasses and the swelling behavior of polymer structures in lignocellulose-containing biomass and of starch in agricultural products was probably underestimated during heating. Swelling is a reversible volume increase of a solid body through exposure to fluids, vapors and gases. The polymer structure swells by means of water inclusion. A physical and chemical swelling process are differentiated. With physical swelling, the water looks for example a place in the pores of the wood and the interspaces. The resulting surface tension between the water and the wood is also called capillary force. In addition to this physical process, a chemical swelling process is present, where water is added to hydrophilic structures as for example OH groups in amino acids. By its hydratizing effect via hydrogen bridges. With plant structures, water is stored between polysaccharides in the cell wall. During the swelling process, gelatin, during the further course also colloidal structures result temporarily, which dissolve again when heated further. Certain albumen substances as for example glue-like substances of bones and skin waste can also swell in water.

Starch occurs in nature in the form of starch granules, which can be elutriated or suspended in cold water. This mainly takes place between 47 and 57° C. At higher temperatures between 55-86° C., the starch granules dissolve. The starch which consists of amylose and amylopectine leaves little by little, for example at 62.5° C. with potato starch and 67.5° C. with wheat starch. The viscosity of the solution thereby increases considerably, and a gel forms. Gels are traditionally also called glues, as they often behave like glues. The entire process of the starch swelling and gel formation is therefore called gelatinization. The starch glue has different stiffening capacities depending on the type of starch. The swelling behavior is increased again by pressure and heat and proceeds in an accelerated manner under the conditions of a thermally induced hydrolysis.

It is known from the literature that the starch part can vary strongly in different biomasses. With maize silage, it can for example be between 1.2 and 44.4 weight percent related to the dry substance. The stiffening capacity of maize starch glue is larger than that of wheat starch glue, and this is again larger than potato starch glue. As maize silage is a biomass used often for generating biomass, the high stiffening capacity has to be especially considered with hydrolysis processes, so as to avoid blockage of heat exchanger systems. It has to be considered that a low starch content of for example below 5 percent can improve the pumpability under certain conditions and especially at constant temperature and pressure ratios. However, as the pressure and the temperature increase very quickly with the thermally induced hydrolysis, a volume increase and thus also an increase of the flow resistance has to be anticipated. Biomass or feed materials with high starch contents of for example over 10-30, 30-50 or over 50 percent related to the dry mass are guided directly into the first reactor via the strand for “dry” biomass, that is, the feed strand I, and are coated there with liquid heated biomass from the feed strand II and/or mixed. Biomass or feed materials having a low starch content below 3, 5 or 10 percent related to the dry mass, which can simultaneously be pumped with or without pretreatment, are guided through the feed strand II.

The cause of the increased formation of deposits and blockages is probably a combination of different factors. The process gas formation in the heat exchanger and the starch swelling play a role in the volume increase. Ideally, a stopper flow is assumed with a tubular reactor. A pressure increase is thus anticipated with a volume increase by gas formation or swelling. This is additionally increased by the increase of the viscosity by starch swelling of the conveyed goods. The flow resistance also increases thereby.

With all plants constructed for the thermal pressure hydrolysis, the heat exchangers formed as tubular reactors were installed horizontally due to the considerable lengths of the straight tube pieces, that is, vertical to the gravitational force. So as to improve the thermally induced hydrolysis or the heating process of biomass, especially with regard to the higher yields related to the solid content, a method for hydrolysis or for heating biomass is suggested with the present invention, which is characterized in that the solid-fluid mixture passes through a heat exchanger for heating and that the solid-fluid mixture is guided through the tube parts which are not curved in an essentially parallel manner to the gravitational force for avoiding caking and/or blockages.

The flowable transported material should move downwards on its own and without considerable impacts of other forces than the gravitational force, so as to prevent baking and blockages. For this, the heat exchanger is designed in such a manner that the amount of the angle of the tube axis to the horizontal plane is larger than 4 or 7 or larger than 10 degrees in the embodiment. The heat exchanger consists of at least 20, 40 or 60 percent of vertical tube parts. Vertical tube parts are the parts of the tubes carrying the media, whose amount of the angle of the tube axis to the vertical plane is at the most 70 or 50 or 45 degrees. Vertical means an angle of below 45 degrees to the vertical, where the angle of the vertical tube parts is at the most 10 degrees to the vertical in the embodiment.

The heat exchanger consists for example of a tubular reactor or a tubular bundle or plate heat exchanger or a combination of these apparatuses. The heat exchanger is designed in a modular manner and can consist of different modules, units or sections. The modular units are arranged in spatial vicinity to each other that several heat exchanger units can be connected in series.

The tempering system of the heat exchanger consists of a double wall, the interspace of which is flown through by a heat energy carrier medium. The heat energy medium is for example a thermal oil, water vapor or process water from the method according to the invention or another process. Different heat carrier media can also be combined. The target temperature of this medium is between 60 and 350° C. The temperature in a first section or module is for example at 60-100 or 80-120° C., in a second section or module between 100 and 140 or 120 and 160° C., in a third section between 140 and 180 or 160 and 200° C., and in a forth section between 180 and 220, 200 and 240, or 240 and 350° C. The temperatures of the heat carrier medium can also be varied up to 20, 40 or 60° C. The units, modules or sections of the heat exchanger are connected in series in such a manner that the temperature of the solid-fluid is brought again to a lower inlet or outlet temperature after achieving a highest or peak temperature of for example 220 to 260° C. The heat exchanger is equipped with a hydrolysis reactor which keeps the material at a level of for example +/−2 to 8° C. and ensures a dwelling time of for example at least 20 minutes corresponding to the regional sanitary regulations.

FIG. 3 shows a schematic depiction of a plant for the thermally induced hydrolysis with a double-stranded feed. The apparatus for the hydrolysis consists of the feed strands I and II and the devolatilization strand III. The strand I serves for conveying feed materials with a high solid content of for example 3 to 50 percent related to the total volume. For this, the “dry” biomass is stored in a hopper 1 and brought to a bottom plate outfeed vessel (2) from there. The feed materials are fed to a comminution apparatus (3) via a conveying device, which can for example be a screw conveyor or a conveyor belt, and are fed from there into a mixing vessel (6).

The dry biomass is mixed thoroughly with concentrated process water from the reservoir (4) and the catalyst dosing feeder (5) in the mixing vessel by means of an agitator. The mixture is fed to the incubation vessel 8 via a further conveying device 7, which can for example be a screw conveyor or a conveyor belt. The incubation vessel enables a residence time of the catalyst on the material. The vessels (7) and (8) are double-walled and have a hot water connection, so as to enable a preheating of the material to 50-60° C.

The incubated material of the “dry” feed materials is fed via the conveyor devices (9) and (10) to the reactor feed apparatus (21). The feed apparatus consists of a force conveyor, which is for example an injector, double screw extruder, an eccentric spiral pump, a piston pump, a spiral displacement pump, which are respectively equipped with or without compressor screws, or a double screw compressor and is provided with stopping apparatuses. The feed apparatus ensures that the incubated material from the strand I with a pressure level above the inner reactor pressure is brought into the reactor (19), and prevents backlashes into the feed device.

Pumpable feed materials with a solid content of 3 to 50 percent related to the entire volume are mixed in the mixing vessel (14) with process water (4) and catalyst (15) via the feed strand II, incubated (16) and are fed to the reactor via a suitable conveyor device (17) (e.g. piston, spiral displacement, or eccentric spiral pump). The material is heated to least 180-200° C. via the heat exchanger unit 18. A single hydrolysis reactor (40) replaces the reactors (19, 24, 32, 33) in FIG. 1 or 2. The elements of the plant otherwise coincide with FIG. 1 or 2, so that they are respectively provided with the same reference numerals. In the hydrolysis reactor (40), fluid, pumpable biomass from the feed strand II is mixed with dry biomass from the feed strand I. The dry biomass from the feed strand I is supplied to the hydrolysis reactor (40) via a suitable introduction apparatus (41). The material can additionally be influenced thermally via a heat exchanger (42) and the double wall (43) of the hydrolysis reactor (40).

After the dwelling time for the reactor (40) has expired, a devolatilization of the material takes place via the heat exchanger (27) into the devolatilization vessel (29). The heat exchanger (27) ensures a cooling of the material to temperatures below the evaporation temperature of water. The passage and the pressure devolatilization are thereby controlled via a backwards-oriented devolatilization pump, which is designed as a force conveyor, eccentric spiral, spiral displacement or piston membrane pump.

The wet feed material is stored in the devolatilization vessel (29). Accumulated heat can be discharged via the double wall. Excess process water is separated via the subsequent solid-fluid separation (30), which is designed as a decanter, centrifuge, cyclone, filter chamber press, filtration or devices used for a similar purpose or described in another part of the specification, and the process water is again made available for other processes within the method according to the invention. The final product is stored temporarily in the store (27) for the further use.

The hydrolysis method is extensively operated in a continuous manner. That is, the period in which feed materials are brought into the process via a reaction cycle or via a heat exchanger unit (18) for the time necessary for the passage of the material, is at least six tenth of the reaction cycle. The same period is valid for the filling process into the heat exchanger (27) for cooling or into the devolatilization vessel (29) in an offset manner. A throughput of the plant is thereby defined via the conveying device (17) and the introduction apparatus (19). The backward-directed devolatilization pump (28) is controlled at different locations of the plant in its rotation speed in such a manner that an evaporation of the material is prevented with the pressure present in the plant. A valve can also be used for devolatilization as an alternative to a devolatilization pump.

The devolatilization apparatus or pump (28) is controlled by temperature and/or pressure. A longer dwelling time in the heat exchanger is achieved via a reduction of the rotation speed. The temperature of the medium is reduced thereby. The temperature is adjusted in such a manner as is necessary in the following apparatus or in the subsequent process. If the reaction mixture is for example guided further into a vessel with ambient pressure, the adjustment to a temperature below the boiling point is necessary, so as to avoid undirected and uncontrolled evaporation processes. Temperatures above the boiling point can be desired with feeding into another drying process, depending on the embodiment some of which are described in another part of this patent specification. The devolatilization pump (28) is controlled in such a manner that the remaining residual pressure is sufficient for the conveyance in a subsequent process or an apparatus. The residual pressure is for example below 10, 5, 2 or 1 bar.

The design of a plant for the thermally induced hydrolysis with a double-stranded feed and the one of a double-stranded feeding apparatus for the method according to the invention are similar in some points. Some apparatuses and design forms can thus be exchanged. All apparatuses in connection with a double-stranded feed material supply are equipped with a control, regulation, automatization to a large extent, as far as possible in a technical and economic manner. The same is valid for all mentioned processes, method or process steps.

The decrease of the viscosity during the course of the method can be seen as a measure of the progress of the hydrolysis. The viscosity of the solid-fluid mixture is reduced when passing through the apparatus for hydrolysis and is reduced to at least three quarters, half or a fifth of the viscosity of the feed material. The adjustment of a solid content as high as possible is necessary to increase the throughput of the feed materials or the yield of the hydrolyzed material. The limiting factor for maximizing the solid content is the pumpability for the mainly wet biomass on the one hand and the conveyability independent of a pump of rather dry biomass connected with introduction into a reactor.

According to the method of to the invention, an additional suspension or dispersion is produced for the production of ceramic materials. The invention relates to a method for the production of an object at least partially with a structure consisting of a ceramic and a carbon-containing material or other substance, of a blank of a carbon-containing material.

The production of articles, such as components or also wear parts, totally or partially of ceramic materials and especially silicon carbide is currently very elaborate, as silicon carbide is a very high-strength substance which can only be shaped or finished mechanically with great difficulty. Silicon carbide is a non-toxic high temperature ceramics which is of high interest especially due to its excellent properties, as amongst others high diamond-like hardness, optical transparence, semiconductor character, high thermal conductivity, chemical and thermal durability, and is thus used in many different areas of engineering, e.g. the production of refractory materials, insulators, and also as semiconductor material. The production of objects of silicon carbide has thereby a high economic importance.

Objects of silicon carbide are usually produced by means of conventional sintering methods, where a compactly ground silicon carbide powder is baked using different bonding agents at high temperatures. The disadvantage of this procedure is the porosity of the resulting objects in addition to the necessary high temperatures and long sintering times, which only allows a use for certain applications.

From DE3322060 is known another production method for objects of silicon carbide, where an object of a carbon-containing material as graphite is produced true to measurement and shape and subsequently, the carbon of the object is replaced by silicon carbide at least near the surface by means of diffusion processes during a long-term annealing treatment. For this, the object is packed into a granulated material of silicon dioxide during annealing, and e.g. hydrogen gas is directed over the granulated material during annealing. By this, a gas with notable silicon monoxide is to be produced, which can then diffuse into the carbon-containing material of the object near the surface and react with the carbon of the object in such a manner that silicon carbide forms in the matrix of the object. By this, an exchange of the carbon of the object with silicon carbide can be achieved at least near the surface, whereby a corresponding improvement of the regions of the object near the surface can be achieved. It is disadvantageous with this procedural method, that the generation of the silicon monoxide gas is elaborate and the necessary amount parts of the silicon monoxide in this gas can only be held and dosed with difficulty. It is thus the object of the present invention to provide improved production methods for objects of ceramic materials and especially silicon carbide, where an object of carbon-containing material or a porous ceramic substance and especially silicon carbide can be converted to silicon carbide totally or partially in a simple and safe manner.

The additional substance suspension or dispersion is obtained by means of the production of a solid-fluid mixture of water and a carbon-containing component as starting or additional component for the production of an insulating and/or ceramic material, wherein the solid-fluid mixture is treated at a temperature of over 100° C. and a pressure of over 5 bar. This is possibly by means of the high purity of the suspension and the extensive elimination of impurities. The sulfur and ash content serves for the characterization of the purity of the additional substance suspension or dispersion, as other parameters such as alkali metals, chlorine, phosphorous, calcium, nitrogen, magnesium, chromium, copper, lead, and zinc behave in a similar manner. By an increased addition or throughput of purified water or process water, the content of the above-mentioned substances in the carbon-containing solid-fluid mixture is reduced correspondingly. The purity of the carbon present in the solid-fluid mixture increases by numerous additional washing steps, which develop a higher efficiency by high pressure and temperature. The sulfur and/or ash content of the solid-fluid mixture is thereby reduced by at least 50% or 75% in relation to the respective original content of the carbon-containing component. The sulfur and ash contents can be reduced by more than 80, 90 or 99% in relation to the respective original content of the carbon-containing component. Or expressed differently, the sulfur and ash content is reduced continuously during the course of the reaction process in connection with washing processes, and it is reduced to over two tenths, one twentieth, or one hundredth of the sulfur and ash content of the feed material towards the end of the process.

The mixture is acidic due to the preincubation in the acidic medium and the addition of acids as catalyst, and thus lends itself for the production of a ceramic material by means of an alkaline sol. The gelation process can be initiated by means of a sol-gel method by adding the acidic additional substance suspension or dispersion to an alkaline sol. A silicon compound and a sol containing organic or inorganic silicates and/or silica result through this treatment method and further method steps. The sol is an aqueous solution of water glass. A carbon component and a silicate component are used for the production of the gel. The gel is heated up to the development of SiC gas until the SiC gas penetrates a provided porous mold. The mold contains purified, pure, highly pure or ultrapure carbon. It is particularly important that the carbon is finely divided in the high-carbon silicon granulated material, that the silicon dioxide immediately reacts with this carbon when the granulated material is heated, and thereby forms a silicon-carbide containing gas, preferably mainly pure silicon carbide gas. A distribution of the carbon in the silicon dioxide can be achieved by the small size of the carbon particles in the additional substance suspension or dispersion, by which the formation of the silicon-carbide containing gas takes place considerably below the normal sublimation temperature of the silicon carbide, especially already at temperatures between 1700° C. and 1900° C. The formed silicon carbide gas can thereby diffuse directly into the object in the described manner. In a further embodiment, it is hereby advantageous if the silicon carbide-containing gas penetrates the object of carbon-containing material in a gaseous manner and displaces the carbon of the object from the carbon matrix. By this, the main component of the matrix of carbon in silicon carbide is exchanged with extensive preservation of the structure of the main component of the matrix, and the properties of the object are changed and improved in the manner already described.

It is an essential advantage for carrying out the method if the carbon-rich silicon granulated material is produced in a sol-gel process with subsequent carbon-thermal reduction. By the use of a sol-gel process for producing the carbon-rich silicon dioxide granulated material, the distribution of the carbon or also of other substances of the granulated material to be added can be adjusted in a very exact and very fine manner, virtually on an atomic basis, whereby the formation of the silicon carbide-containing gas is improved or will be enabled to a larger scale for the first time. By the fine distribution of the carbon and the other substances of the granulated material to be added, the silicon oxide-containing gas forming during the annealing process can immediately react with the carbon and the other substances to be added, and is immediately available for the diffusion processes near the surface of the object.

From DE 102006055469 is known a method for producing an object, where the object is manufactured from a blank at least partially with silicon carbide structure from a carbon-containing material, wherein the object of the carbon-containing material is manufactured in a first step according to its desired final shape and/or final measurements, and subsequently the object of carbon-containing material is surrounded at least in regions with a carbon-rich silicon dioxide granulated material and is annealed at least once in this enclosure in a protective gas atmosphere at an annealing temperature, where the silicon dioxide granulated material discharges silicon-carbide-containing gas which penetrates the object and converts the carbon-containing material partially or totally into silicon carbide.

It is advantageous if the sol-gel process uses a soluble hydrolyzable inorganic or organic silicate as staring product for producing the carbon-rich silicon dioxide granulated material. A large number of feasible starting substances are comprised herein, which are available as silicon supplier for forming the granulated material and can be used favorably in the sol-gel process. The following explicitly given substances are hereby only agents of the previously mentioned substance classes and cannot be seen as a concluding listing of substances to be used. Water-soluble alkali silicates such as water glass can be used as starting substances for the sol-gel process with the inorganic silicates.

LIST OF REFERENCE NUMERALS

1 Hopper

2 Vessel

3 Comminution device

4 Reservoir

5 Container

6 Mixing vessel

7 Conveying device

8 Incubation vessel

9 Conveying device

10 Conveying device

11

12 Storage container

13 Conveying apparatus

14 Mixing vessel

15 Container

16 Incubation vessel

17 Conveying apparatus

18 Heat exchanger unit

19 Reactor

20 Stirring apparatus

21 Introduction device

22 Heat exchanger apparatus

33 Double wall

24 Reactor

25 Heat exchanger unit

26 Devolatilization

27 Heat exchanger

28 Devolatilization pump

29 Devolatilization vessel

30 Solid-fluid separation apparatus

31 Store

32 Reactor

33 Reactor

34

35

36

37

38

39

40 Hydrolysis reactor

41 Introduction device

42 Heat exchanger

43 Double wall

Claims

1.-20. (canceled)

21. Method for the production of fuels from a solid-fluid mixture of water and a carbon-containing component, wherein the solid-fluid mixture is treated at a temperature of over 100-300° C. and a pressure of over 5 bar,

characterized in that

non-pumpable starting substances are conveyed in the reactor via a first conveyor line, and, parallel or offset therefrom, pumpable heated starting substances are conveyed in at least a first reactor via a second conveyor line.

22. Method according to claim 21, wherein non-pumpable starting substances with a solid content of 25 to 97 percent related to the total volume are conveyed in the reactor via a first conveyor line and, parallel or offset therefrom, pumpable heated starting substances with a solid content of 3 to 50 percent related to the total volume are directed via a second conveyor line.

23. Method according to claim 21, wherein the ratio of the mass throughput of non-pumpable to pumpable starting substances is 1:20 to 10:1.

24. Method according to claim 21, wherein the non-pumpable starting substances are conveyed to the reactor from the first conveyor line under a pressure above the vapor pressure of the process water and are coated with pumpable starting substances from the second conveyor line.

25. Method according to claim 24, wherein the conveyor device for adding the non-pumpable starting substances from the first conveyor line into the reactor under pressure above the vapor pressure of the process water is an injector, a double screw extruder, an eccentric spiral pump, a piston pump which are respectively equipped with or without a spiral compressor, or a double spiral compressor.

26. Method according claim 21, wherein the ratio of the mass throughput of provided to added starting substances is 1:20 to 10:1, or 1:5 to 1:1.

27. Device for treating a solid-fluid mixture of water and a carbon-containing component at a temperature of over 100-300° C. and a pressure of over 5 bar, comprising a reactor,

characterized in that

the device comprises a feeding apparatus with the following devices: a. a first conveyor line conveying pumpable starting substances solid-liquid mixtures with a solid content of 3 to 50 percent related to the total volume, and b. a second conveyor line conveying for conveying non-pumpable starting substances with a solid content of 25 to 97 percent related to the total volume.

28. Method for the production of materials or fuels, humus, Maillard or similar reaction products from a solid-fluid mixture of water and a carbon-containing component, wherein the solid-fluid mixture is treated at a temperature of 100 -300° C. and a pressure of over 5 bar,

characterized in that

enriched process water is used for preincubation, preheating of starting substances, production of the pumpability of a solid-fluid mixture, for take-over into the reaction mixture, for coating or admixing to provided starting substance in a reactor of the plant, for returning into the running process, as heat carrier medium, for further processes within or outside a plant or as a fertilizer component.

29. Use of enriched process water from a method for the production fuels from a solid-fluid mixture of water and a carbon-containing component, wherein the solid-fluid mixture is treated at a temperature of 100-300° C., a pressure of over 5 bar and a treatment time of at least 1 hour,

for

preincubation, preheating of starting substances, production of a pumpable solid-fluid mixture, for the takeover into the reaction mixture, for coating of or mixing to the given starting substance in a reactor of the plant, for returning into the running process, as heat carrier medium or as fertilizer component.

30. Apparatus for the production of fuels from a solid-fluid mixture of water and a carbon-containing component and for treating the same, wherein the solid-fluid mixture is treated at a temperature of 100-300° C., a pressure of over 5 bar and a treatment time of at least 1 hour,

characterized by

an apparatus for the enrichment of withdrawn process water and for returning the enriched process water to the solid-fluid mixture.