WO2019001921A1

WO2019001921A1 - Method and device for generating coal from biomass by means of hydrothermal carbonisation

Info

Publication number: WO2019001921A1
Application number: PCT/EP2018/065015
Authority: WO
Inventors: Datcho Datchev
Original assignee: Mitsubishi Hitachi Power Systems Europe Gmbh
Priority date: 2017-06-29
Filing date: 2018-06-07
Publication date: 2019-01-03
Also published as: DE102017114599A1

Abstract

In a method for generating coal (5) from biomass (4) by means of hydrothermal carbonisation in an autoclave (1), wherein the reaction chamber (2) inside the autoclave is filled with biomass (4) to be carbonised in batches at the beginning of every carbonisation cycle involving the conversion of the biomass (4) into coal (5), wherein the carbonisation reaction of the biomass (4) in the autoclave (1) is carried out in an atmosphere at least predominantly formed of water vapour, and the carbonisation is caused by increased-pressure water vapour introduced into the biomass (4), a solution is created which provides improved steam generation for carrying out a hydrothermal carbonisation of biomass to form coal in an autoclave. This is achieved in that the increased-pressure water vapour causing the carbonisation of the biomass (4) is generated during the respective carbonisation cycle, at least periodically in the reaction chamber (2) of the autoclave (1) arranged inside the autoclave and filled with biomass (4) to be carbonised, by means of at least one evaporator (31) arranged and designed therein.

Description

Method and apparatus for producing coal from biomass by hydrothermal carbonation

The invention is directed to a process for the production of coal from biomass by means of hydrothermal carbonization in an autoclave, the autoclave inside reaction space is filled at the beginning of each carbonation cycle comprising the conversion of the biomass in coal with biomass to be carbonized, wherein the carbonization reaction of the biomass in the Autoclave carried out in an at least predominantly steam atmosphere and the carbonization is effected by means of introduced into the biomass steam increased pressure.

Furthermore, the invention is directed to an autoclave for producing coal from biomass by hydrothermal carbonation in an at least predominantly steam-shaped medium, the autoclave inside reaction space for carrying out the hydrothermal carbonization is partially filled with reaction and / or process water and batchwise with biomass to be carbonized, and in which the carbonization reaction of the biomass can be carried out in an at least predominantly vaporous atmosphere and by means of increased pressure of steam introduced into the biomass, and the one comprising the biomass-receiving container and positioned in the autoclave during a carbonization cycle.

Finally, the invention is directed to a plant for the production of coal from biomass by means of hydrothermal carbonization under elevated pressure in an at least predominantly steam-shaped medium, in particular for carrying out the method defined above.

For some years, methods and devices have been developed to, in principle, any available, natural biomass by the process of "hydrothermal carbonization" (HTC) coal, so-called biochar or

In its origin, the HTC (hydrothermal carbonization) process is that the raw biomass (wood, parts of plants, eg straw, plant residues, etc.) in a pressure-resistant reaction vessel (autoclave) filled and here in an autoclave inside Reaction space is immersed in a water bath. The contents of the reaction space are brought to elevated temperature and pressure, so that the biomass carbonation process takes place. Subsequently, the reaction space is emptied and the generated biochar or biochar from the water or process water is filtered, mechanically dewatered and treated before it is then sent for further use.

Further developments of this process are that the carbonation reaction or the carbonization process does not take place exclusively in a liquid, but predominantly or exclusively in a gaseous, in particular vaporous, medium. In this case, heat is supplied to the reaction space by means of hot gas or heating steam (saturated steam or superheated steam). For example, the carbonization process is operated at a temperature of 180 ° C and an autoclave inside vapor pressure of 10 bar. In contrast to the original hydrothermal carbonization (HTC), in this process the volume of the autoclave interior reaction space not filled by the biomass is not completely filled with water during one carbonation cycle but filled with steam at the top and hot water at the bottom or none Liquid phase to a significant extent but only hot gas or water vapor in the reaction vessel. These methods are referred to as vapohydrothermal carbonation (VHTC) or, in the presence of a single vapor phase, as vapothermal carbonation (VTC). However, these methods continue to represent embodiments that are subsumed under the generic term "hydrothermal carbonization" (HTC), which is why in the present application, only a method for hydrothermal carbonization is mentioned, although the carbonation reaction and the carbonation process in a predominantly or To accelerate the carbonation process, the steam or other involved

Water of reaction, a catalyst, such as citric acid, are added. Such a method is known from DE 10 2009 010 233 A1. In this method, the steam outside of the pressure-tight container (autoclave) is generated by means of a steam generator. The hot steam is introduced into the autoclave inside reaction space and the biomass located there and led out to form a steam / condensate cycle from the autoclave and after treatment in a wastewater treatment or wastewater treatment then partially fed back to the steam generator and this in turn as steam in the autoclave and introduced the autoclave inside reaction space. Here, first clean steam is generated, which is then contaminated after flowing through the biomass and exit as steam / condensate from the autoclave. This "contaminated" by the biomass steam or condensate, which has also increased in volume by water absorption from the biomass, then has to be cleaned consuming, before then a purified steam / condensate fraction in turn fed to the steam generator to produce new live steam can.

In practice, therefore, this method has already been further developed in that a steam generator which processes exclusively "clean" steam and condensate is connected with its water / steam circuit to a heat exchanger arranged outside of an autoclave. Condensate cycle, where in the heat exchanger with the aid of the steam supplied by the steam generator "contaminated" steam is generated.This steam is then in the way of the "contaminated" steam / condensate circuit from the outside in an autoclave inside reaction chamber of the autoclave and in the biomass Initiation of the carbonation reaction and carbonization initiated. The resulting wastewater is treated and purified, creating a "contaminated" condensate or wastewater, which is then at least partially recycled to the external heat exchanger by way of "contaminated" steam / condensate circuit for evaporation in the "contaminated" steam. In the case of all the systems enabling these process variants, the respective steam generators required for the carbonization are therefore located outside the pressure vessel or autoclave. Likewise, a heat exchanger in line connection with a respective steam generator and generating steam for use in the autoclave or pressure vessel is located outside the autoclave or pressure vessel. In other words, the steam required for carrying out the carbonation reaction is generated exclusively outside a respective autoclave or reaction vessel receiving and / or containing the biomass to be carbonized in the hydrothermal or vapothermal carbonization processes considered here. This requires appropriately sized steam generators and / or heat exchangers, which produce a steam sufficiently high temperature and associated higher pressure, for example, greater than 180 ° C and greater than 10 bar, and can supply the pressure vessel or autoclave line. Such units must therefore have corresponding pressure-resistant lines and pressure vessels, so that their production is technically relatively complex and therefore expensive.

The invention is therefore based on the object to provide a solution which provides improved steam generation for carrying out a hydrothermal

Carbonization of biomass to coal in an autoclave provides.

In a method of the type described in more detail, this object is achieved in that the carbonization of the biomass causing water pressure increased pressure during the respective carbonization at least temporarily in the filled with the biomass to be carbonized autoclave inside reaction space of the autoclave by means of at least one therein formed and arranged evaporator is produced. Likewise, the above object is achieved in an autoclave of the type described in more detail by the fact that the autoclave inside reaction chamber has an evaporator. Finally, the object is achieved by a plant for the production of coal from biomass by means of hydrothermal carbonization under elevated pressure in an at least predominantly steam-shaped medium, in particular for carrying out a method according to one of claims 1-8, which several, with their respective autoclave inside reaction chambers in steam autoclave according to one or more of claims 9 - 22, one or more with at least the autoclave inside reaction space of one of the autoclave in steam-conducting line connection standing (n) heat accumulator and one or more with a steam generating unit, in particular a heat energy coupling part, an autoclave inside heat exchanger arranged Has at least one of the autoclave in vapor-conducting line connection standing (s) steam generator. Owing to the procedure according to the invention of generating the water vaporization of the autoclave in the autoclave interior reaction space of the autoclave by means of an evaporator formed and arranged in the autoclave interior reaction space, improved steam generation is provided for carrying out a hydrothermal carbonization of biomass to coal in an autoclave.

It is now possible to use evaporators or heat exchangers with integrated steam generation unit which themselves do not require their own pressure vessels or pressurized lines, since the autoclave inside the reaction chamber surrounding them or the surrounding pressure vessel or autoclave provides the required pressure vessel. The built-in autoclave evaporator or heat exchanger can therefore be designed and constructed structurally simpler and thus cheaper to produce than previously required external heat exchanger. Furthermore, both the heat exchanger and a water vapor generating unit are arranged in the autoclave inside reaction space, so that no long connecting lines between steam generator or

Steam generator unit and heat exchanger are more necessary, which also to a technically less expensive and therefore cheaper Implementation of the steam supply for carrying out a hydrothermal or vapothermal carbonization brings with it. Due to the no longer present long or at least longer steam lines, the energy losses between steam generator or steam generating unit and heat exchanger are improved compared to the embodiments of the prior art, so that the inventive solution is energetically favorable.

Furthermore, results from the inventive arrangement of the evaporator, in particular the heat exchanger with steam generating unit in the autoclave inside reaction space in which runs the hydrothermal carbonation reaction, the possibility of the prior art before the initiation of emerging condensate in municipal sewage treatment plants necessary wastewater treatment or wastewater treatment in the autoclave embarrassed and integrated in the ongoing process of hydrothermal carbonization, as will be explained in more detail below. The thermal energy introduced by the evaporator or heat exchanger integrated into the autoclave interior reaction space can be used to generate the steam necessary for the course of the hydrothermal carbonization reaction, but also during the hydrothermal carbonization process in the autoclave inside

Reaction vessel wastewater into sewage sludge and contaminated clear condensate to divide. The Klarkondensat formed during the HTC process can be introduced directly into conventional, for example, municipal, sewage treatment plants, without the need for a previous additional process water or Klarkondensataufbereitung or treatment.

Overall, the elimination of one or more external heat exchanger (s) and the shorter connecting lines results in a compact and cost-effective design of an autoclave suitable for carrying out a hydrothermal carbonization. In addition, a process water or condensate treatment plant is no longer necessary. In addition, the fact that the reaction water emerging from the biomass in the autoclave interior reaction chamber during a carbonation cycle is used directly in the reaction space to form steam for the hydrothermal carbonization, the amount of water produced is reduced because of a additional steam injection or steam injection is dispensed into the autoclave.

The evaporator or heat exchanger can be connected via lines with an external, for example in the context of industrial plants steam generator, which fed him in the circuit on the one hand steam and this is discharged after extraction of heat energy on the other side as condensate. In particular, when the autoclave is interconnected with a plurality of autoclaves of the same type to a uniformly cooperating overall plant, it is expedient and advantageous for the implementation of the method if the water vaporization of the biomass causing increased pressure during the respective carbonization cycle at least for a period of time at least 30% of the time of a carbonization cycle, during which water vapor of elevated pressure in the autoclave interior reaction space is required for the course of the carbonation reaction, is generated by means of the at least one evaporator arranged therein, which the invention also provides in the development of the process.

Overall, ie related to a particular carbonization cycle, it is advantageous and expedient according to the invention, when the carbonization of the biomass causing water pressure increased pressure during the respective carbonization cycle substantially and / or predominantly in the filled with the biomass to be carbonized autoclave inside reaction space In this context, essentially or predominantly means that steam is generated on the inside of the autoclave by means of the evaporator for more than 50% of the time of a carbonization cycle, and / or that an amount of more than 50% is produced % By weight of the steam needed or consumed during a carbonation cycle is produced on the inside of the autoclave by means of the evaporator. In order to be able to produce the carbonization of the biomass causing water vapor advantageously in the autoclave inside reaction chamber of the autoclave, it is advantageous according to the embodiment of the method, if the steam generated in the autoclave inside the reaction chamber of the autoclave by means of a arranged in the autoclave inside the reaction chamber of the autoclave heat exchanger assigned, in particular integrated, and arranged in the autoclave inside the reaction chamber of the autoclave water vapor generating unit is generated. For the economy of the system and in particular the further optionally necessary treatment of the forming during the process condensate, it is useful if the condensate is divided into a cloudy condensate, the suspended solids and sludge or sewage sludge constituents, and this sludge or sewage sludge non-exhibiting Klarkondensat , The process according to the invention therefore provides, in a further development, for liquid emerging from the biomass during the carbonization cycle to form a liquid formed in the autoclave interior reaction space

Convapor condensate collecting space is supplied and / or running on the inner wall regions of the autoclave inside the reaction chamber condensate formed in the autoclave inside reaction space

Clear condensate collecting space is supplied.

Due to the fact that the evaporator or the heat exchanger with its steam generation unit is arranged on the inside of the autoclave, this steam generating unit can be used to collect and evaporate reaction water or turbidity condensate leaving the biomass. In this evaporation then remain the suspended matter or sludge or sewage sludge components in the water vapor generating unit and only the water-containing and / or liquid components (eg, resulting / resulting acetic acid can be evaporated) evaporated. This vaporized original turbidity condensate then condenses partly on the inner walls surrounding the autoclave interior reaction space and is here - due to the no longer contained therein suspended solids or sludge and sewage sludge constituents - precipitated as Klarkondensat. This Klarkondensat then runs along the walls and can in a Clark condensate collection space in the autoclave inside reaction space are collected.

Since biomass of various kinds can be converted into biochar or biochar in an autoclave according to the invention, biomass of different water content is used. This may result in more water being released from the biomass during a carbonation cycle than is actually necessary to produce the steam needed to carry out the hydrothermal carbonation reaction. That is, more steam is generated than actually necessary. This can be compensated and used by connecting several autoclaves parallel to each other and each being in different time phases of the hydrothermal carbonization cycle. This can be used to ensure that excess steam arising or generated in an autoclave is supplied to a second autoclave of the parallel-connected autoclave which is still in the initial phase of a hydrothermal carbonization cycle, for example. The invention therefore also provides in a development that a portion of the water vapor of the autoclave inside the reaction chamber carbonization cycle, in particular at the beginning of the carbonization cycle, the autoclave inside reaction space of one or more parallel autoclave of the same type is supplied and / or that a portion of the water vapor of the increased pressure resulting in the carbonization of the biomass is supplied to the autoclave-side reaction space of a parallel-connected autoclave of the same type during the respective carbonization cycle taking place in the autoclave interior reaction space.

But it is also possible to use resulting excess steam in a connected to the respective autoclave or the parallel group of autoclaves heat storage. Therefore, in an embodiment of the method according to the invention, the invention is also distinguished by the fact that part of the water vapor which causes the carbonization of the biomass has increased pressure during the respective reaction chamber in the autoclave inside expiring carbonation cycle, in particular at the beginning of the carbonization, the autoclave inside reaction chamber is supplied from a heat storage and / or that a portion of the carbonization of the biomass causing water vapor pressure is supplied during the respective running in the autoclave inside reaction space carbonation cycle from the autoclave inside reaction chamber a heat storage.

In order not to be able to produce steam which is not required in the autoclave interior reaction space for the hydrothermal carbonization process, and in particular to be able to tailor steam production specifically to the water content introduced with the biomass to be subjected to a carbonization cycle, it is advantageous according to a further embodiment of the process according to the invention the autoclave inside reaction space at the beginning of each carbonization cycle comprising the conversion of the biomass into coal is not or only partially and partially filled with water of reaction to be evaporated.

Thus, only so much water is introduced into the autoclave interior reaction space that on the one hand the biomass is not immersed in a water bath and on the other hand preferably generates the steam required exclusively from the registered with the biomass amount of water and / or possibly as a parallel-connected autoclave or provided steam is supplied from a heat accumulator. For carrying out the method explained above and the advantages that can be achieved therewith, it is particularly advantageous that the evaporator has a heat exchanger with associated, in particular integrated, and arranged in the autoclave inside reaction space

Steam generating unit comprises, in particular designed as such, whereby the autoclave is distinguished in development.

The autoclave is also characterized in an embodiment in that the heat exchanger decouples heat energy supplied to the water vapor generation unit. The for the evaporation of water necessary heat energy can be provided in this way by means of a heat carrier fluid supplied externally, in particular as generated by an external steam generator steam. According to a development of the invention, a particularly compact and advantageous embodiment of a heat exchanger with integrated steam generating unit can be provided in that the heat exchanger comprises a thermal energy coupling part which can be flowed through by a heat carrier fluid, preferably heat pipes, and which couples thermal energy to the steam generating unit, in heat-conducting connection with the steam generator unit stands.

In this case, it is furthermore expedient if the water vapor generating unit is designed as a unit integrated in the heat exchanger and its heat energy coupling part and formed on the top side on the heat energy coupling part in the form of a, in particular hydrous, liquid-holding trough, which the invention furthermore provides. In this embodiment, the trough can be formed, in particular, as a sump pan formed below the container holding the biomass, into which reaction water and turbidity condensate emerging from the biomass is collected. This water of reaction exiting from the biomass during the hydrothermal carbonation process exits as a turbid condensate provided with particulate matter or sludge components or sewage sludge constituents. This turbidity condensate is collected in the tub or sump and vaporized during the ongoing hydrothermal carbonation process due to heat energy input from the heat energy coupling part of the heat exchanger again. The suspended solids and sludge or sewage sludge components in the tub or sump remain, while the other condensate constituents, in particular the hydrous constituents, evaporate. These then strike, inter alia, at the walls of the reaction space surrounding the autoclave inside the reaction space, which at the same time can also be the walls of the autoclave, down and condense there, since they no longer contain any suspended matter or sludge or sewage sludge constituents, as clear condensate. With the embodiment according to the invention and in particular the configuration of the heat exchanger with associated or integrated trough or sump well, a wastewater treatment can be carried out simultaneously in the autoclave and in the autoclave inside reaction space with the running hydrothermal or vapothermal carbonization process, the turbidity condensate formed during the carbonation process at least partially, preferably predominantly and mostly, recycled to a clear concentrate. The cloudy condensate collected or collected in the tub or sump pan can be freed from the turbulences by the evaporation taking place here and can be obtained as a condensate by condensation on the inner walls or inner walls of the reaction space or of the autoclave. For this purpose, it is of particular advantage if the water vapor generating unit of the heat exchanger, preferably the heat energy coupling part and the water vapor generating unit of the heat exchanger, are arranged in the autoclave inside reaction space below the receiving the biomass to be carbonized container and at a distance from the autoclave inside bottom surface of the reaction chamber, whereby the invention also distinguished. This makes it possible, on the one hand, to collect turbidity condensate leaving the biomass and, on the other hand, to collect undiluted clear condensate below the steam generating unit. In order to be able to supply the reaction water or turbid condensate leaving the biomass to the steam generating unit, in particular the tank holding the liquid, the autoclave is further characterized by the fact that the water steam generating unit is assigned means that its water of reaction emerging from the biomass during the carbonization cycle or add turbidity condensate.

Particularly expedient means present at the biomass holding and receiving container arranged, liquid-conducting baffles, so that the invention further provides that the means associated with the water vapor generating unit are designed as baffles which form wall regions of the container and supply liquid to the liquid-receiving and / or holding region of the trough.

Preferably, the liquid receiving or holding region of the trough or sump is a turbidity condensate collection so that the autoclave according to the invention is further characterized in that the water vapor generating unit, in particular the liquid receiving and / or holding portion of the tub, one from the biomass exiting liquid, in particular reaction water and / or turbidity condensate, forming Trübkondensatsammelraum forms.

The forming Klarkondensat is suitably collected in a preferably formed below the evaporator or heat exchanger in the autoclave inside reaction chamber Klarkondensathammelraum. The autoclave is therefore also characterized in an embodiment in that in the wall region of the autoclave inside the reaction chamber, in particular below the evaporator, preferably below the steam generator unit of the heat exchanger, in particular below the

Tray, particularly preferably below the heat energy coupling part, a condensate condensing on the inner wall regions of the autoclave inside the reaction space and draining condensate receiving Klarkondensathsammelraum is formed.

In order to be able to conduct the liquid respectively collected from the turbidity condensate collecting chamber and the clear condensate collecting space out of the autoclave, the invention further provides that the turbidity condensate collecting space carries a condensate removal line leading out of the autoclave and / or the clear condensate collecting space leading out of the autoclave

Clark condensate removal line comprises.

Since, according to the invention, the amount of steam required for carrying out a carbonization cycle is at least substantially and preferably predominantly exclusively within the autoclave interior reaction space and thus to produce within the autoclave, it is helpful if the arranged in the autoclave or in the autoclave inside reaction chamber evaporator or arranged in the autoclave or in the autoclave inside reaction chamber steam generation unit is designed accordingly. The invention therefore provides in a further embodiment of the autoclave, that the evaporator, in particular the heat energy coupling part and the water vapor generating unit of the heat exchanger, are designed so that the required for the batch execution of a carbonization cycle of the introduced with the container biomass in the autoclave inside reaction space water vapor amount at least Substantially, preferably predominantly, if desired completely, in the autoclave inside reaction space can be generated. Substantially or predominantly in this context means that an amount of more than 50% by weight of the amount of steam required or consumed / consumed during a carbonation cycle can be produced on the inside of the autoclave by means of the evaporator and thus can be produced.

Since the autoclave can be filled and operated with a wide variety of biomass, it may be that such a water content is introduced into the autoclave interior reaction space with the biomass, that the amount of steam producible therefrom, at least in phases, during a carbonation cycle is greater than that currently for the carbonization required amount of steam. In order to still be able to use such an "excess" vapor quantity, it is expedient if a plurality of autoclaves are connected to one another via a steam-conducting line and, in particular, are arranged connected in parallel. Such a steam line can preferably be a vapor-displacement line, so that the invention further provides, in an embodiment of the autoclave, that the autoclave is connected to a vapor-displacement line, via which its autoclave-interior reaction space with the autoclave inside

Reaction space of at least a second autoclave of the same type and / or a heat storage is connected. Since the biomass in the container, with which it is introduced into the autoclave inside reaction space, may be compressed, there is a possibility that the steam penetration depth and Vampstof Penetration possibility of the steam is impeded in the biomass due to the compacted bulk material. To counter this problem, the invention finally also provides in a further embodiment of the autoclave that a plurality of steam guide tubes extending therethrough and at least one end, preferably both ends, are provided for incoming steam and perforated in their tube wall. This makes it possible for water vapor forming in the autoclave inside the reaction chamber to flow into it from one or both open ends of a steam guide tube and then to flow through the perforated tube wall into the biomass surrounding the tubes. In this way, the penetrating depth to be managed by the steam can be improved by virtue of the fact that the steam no longer has to flow from the outside of the container into the center of the container, but this path is optimized by the corresponding arrangement of the steam guide tubes. At the same time, these steam guide tubes also serve as drainage pipes for reaction water and turbidity condensate forming in the biomass. The invention is explained in more detail below by way of example with reference to a drawing. This shows in:

Fig. 1 in a schematic representation of a flow chart of the method according to the invention

2 is a schematic representation of a cross section through an autoclave according to the invention,

Fig. 3 is a schematic representation of a longitudinal section through the

Evaporator of the autoclave shown in FIG. 2 and in

Fig. 4 shows a schematic representation of an inventive system. The inventive method illustrated in FIG. 1 in the form of a schematic flow diagram comprises as its core an autoclave 1 which has an evaporator 31 in its autoclave-side reaction space 2. This makes it possible for the steam of increased pressure required for the carbonization of biomass 4 introduced into the autoclave interior reaction chamber 2 to be at least temporarily, preferably substantially and / or predominantly, in the autoclave inside reaction space 2 of the biomass 4 to be carbonized during a particular carbonization cycle Autoclave 1 to produce. The terms "substantially" and "predominantly" are intended to express that it is in principle possible to generate the entire required steam completely within the autoclave inside reaction space, but that it may be appropriate and useful under certain conditions, external steam of As is explained further below, "essentially" and "predominantly" means that in each carbonization cycle, either during the predominant time of an entire respective carbonization cycle, the steam in the inner side of the autoclave Reaction space 2 is generated and not supplied from the outside or discharged to the outside or that at least the largest part of the required during a carbonization cycle steam is generated in the autoclave inside reaction chamber 2. In this context, essentially or predominantly means that steam is generated for more than 50% of the time of a carbonization cycle on the inside of the autoclave by means of the evaporator, and / or that a vapor quantity of more than 50% by weight is required or consumed during a carbonation cycle. processed (water) steam autoclave inside by means of the evaporator is generated. At least, however, temporarily, ie for a period of time which is at least 30% of the time of a carbonization cycle during which increased steam pressure in the autoclave interior reaction space 2 is required, this water vapor increased pressure in the autoclave inside reaction space 2 by means of at least one evaporator 31, in particular a heat exchanger or heat exchanger 3 with a water vapor generating unit 11 generates. In the autoclave inside reaction chamber 2 of the autoclave 1 biomass 4 is introduced batchwise and then converted in a carbonization cycle to biochar or biochar or "Green Coal" 5. In the autoclave 1 and in the autoclave interior reaction chamber 2 formed in addition to the biochar 5 as end products a sewage sludge 6 and a contaminated Klarkondensat 7. While the biomass 4 is added batchwise and the biochar 5 and the sewage sludge 6 preferably batchwise after completion of a carbonization cycle the autoclave 1, the contaminated Klarkondensat 7 can be continuously derived during a carbonation cycle and fed directly to a municipal sewage treatment plant In order to provide the heat energy necessary for the evaporation of water within the autoclave interior reaction space, the evaporator 31 comprises the heat exchanger 3, which via a steam / condensate circuit 9 with an external steam generator 8 is connected. The external steam generator 8 supplies heat to the heat exchanger 3, which decouples heat energy in the autoclave-side reaction space 2, condenses here and then is recycled as condensate back to the steam generator 8. With the autoclave 1 according to the invention, vapor production with carrying out a carbonization cycle and with integrated process water or reaction water treatment can be carried out on account of the evaporator 31 arranged in the autoclave interior reaction chamber 2. With the aid of the heat exchanger 3 comprehensive evaporator 31 steam is produced with the required temperature and the required pressure in the autoclave inside reaction chamber 2 and thereby carried out a treatment of the resulting during a carbonization cycle as turbidity condensate 18 reaction water. This is achieved in that the reaction water or process water occurring during the carbonization cycle is vaporized by means of the evaporator 31 comprising the heat exchanger 3 to the respectively required steam.

A carbonization cycle includes the steps: a) loading of the autoclave inside reaction chamber 2 of the autoclave 1 with biomass 4;

b) Generation of water vapor in the autoclave interior reaction space 2 and / or supply of water vapor in the autoclave inside reaction space 2;

c) carrying out the carbonization process and thereby collecting and vaporizing the turbidity condensate 18 leaving the biomass 4 during the carbonization cycle;

d) collecting condensate condensing on wall regions of the autoclave-side reaction space 2 during the carbonization process as contaminated clear condensate 7, preferably in the bottom region of the autoclave-side reaction space 2 of the autoclave 1, and

e) after sufficient holding time and conversion of the biomass 4 into biochar 5 removal of the biochar 5 and the sewage sludge 6 and optionally the contaminated clear condensate 7, if the latter has not already been continuously discharged during the carbonation cycle.

Hereby, in order to carry out step e) after completion of the actual carbonation reaction of the hydrothermal carbonation process, i. after the end of the holding time, the pressure in the autoclave 1 is reduced to atmospheric pressure, so that the autoclave 1 can be opened and the biochar 5 and the sewage sludge 6 removed. A renewed carbonization cycle then begins with a recharging of the autoclave 1 with a container 16 filled with biomass 4.

An autoclave 1 suitable for carrying out the process according to the invention is shown schematically in cross-section in FIG. In the illustrated here autoclave 1 with a round cross section may be a pressure vessel, as it is known for example as a cylindrical autoclave from the lime sandstone production. In the autoclave interior reaction chamber 2 of the heat exchanger 3 comprehensive evaporator 31 is arranged at a distance from the bottom region of the autoclave wall 10 in the lower part of the autoclave inside reaction chamber 2. The heat exchanger or heat exchanger 3 comprises a water vapor generating unit 1 1 and a heat energy coupling part 12, wherein the water vapor generating unit 1 1 is formed on the upper side on the heat energy coupling part 12 in the form of an upper side open, water-containing liquid-holding pan 13. The water vapor generating unit 1 1 and the heat energy coupling part 12 are formed as a heat exchanger 3 forming unit.

The one or more thermal energy coupling part 12 is constructed in the embodiment of several so-called omega-tubes 14, which directly form the bottom surface of the trough 13 on its side facing the water vapor generating unit 1 1 and are surrounded in the other areas outside of a thermal insulation 15. But it is also possible that the top of the omega tubes 14 does not directly form the bottom of the tub 13, but that rests on this top a tub bottom.

The flow cross-section of the omega tubes 14 is connected to the steam / condensate circuit 9 of the external steam generator 8, so that the omega tubes 14 are traversed or flooded by steam. During the passage of the heat energy coupling part 12, this steam of the steam / condensate circuit 9 emits heat energy, which is the

Thermal energy coupling part 12 to the steam generating unit 1 1 decouples or forwards. The then in the flow cross section of the Omega tubes 14 condensing steam is then recycled as condensate to the external steam generator 8. Of course, other tube shapes for the formation of the heat energy coupling part 12 and the supply of steam can be used instead of the omega tubes 14 described in the embodiment.

Above the upper-side opening of the trough-shaped trough 13, a container 16 filled with the biomass 4 to be carbonized is arranged to carry out a carbonization process. in the

Embodiment, the container 16 is even placed directly on the edge region of the trough-shaped trough 13. The container 16 is in the form of a basket and comprises or contains the biomass 4. The container 16 is for the most part perforated or lattice-shaped in its wall area, which is shown in FIG 2 by the biomass 4 surrounding dashed line is indicated. In the lower third of its wall region, however, the container 16 is provided with closed, liquid-conducting wall regions or baffles 17, which are indicated as a solid line. These baffles 17 taper the cross-section of the container 16 such that its bottom-side opening is positioned above the opening of the trough-shaped tray 13. The positioning of the container 16 shown in FIG. 2 is that in which it is introduced into the autoclave 1 for carrying out a hydrothermal carbonization process and positioned there for a carbonization cycle. The baffles 17 thereby represent means which supply the water vapor generating unit 11 or the tub 13 during a Carbonisierungszyklus from the biomass 4 emerging reaction water or turbidity condensate 18 or forward. Process or reaction water leaving the biomass 4 during a carbonization cycle is thus collected as so-called turbidity condensate 18 in the tub 13. The tub 13 thus also forms a turbidity condensate collection chamber 19 or a sump tray. The process or reaction water or turbidity condensate 18 collected in the trough 13 or possibly added at the beginning of a carbonation process is vaporized by the thermal energy provided by the steam supplied to the thermal energy coupling part 12 by the external steam generator 8, thereby making it necessary for the hydrothermal carbonation reaction to proceed Steam in the autoclave inside reaction space 2 - at least substantially and / or predominantly - ready. This vapor penetrates into the biomass 4 and reacts with the biomass 4 in the context of the carbonization reaction to the biochar 5. Resulting reaction water or condensate is recycled as turbidity condensate 18 in the tub 13.

A portion of the vapor condenses on the inner wall regions of the autoclave wall 10 and then runs along this to the lowest point of the autoclave interior reaction chamber 2 and collects there as contaminated Clarkondensat 7. This deepest portion of the autoclave inside reaction chamber 2 thus forms a Klarkondensathsammelraum 21 from. The evaporation of the turbidity condensate 18 can be adjusted such that at the end of the carbonization cycle in the tub 13 the sewage sludge 6 is present, to which the turbid condensate 18 has been processed by evaporation and leaving behind suspended matter or sludge during the carbonization cycle. This sewage sludge 6 can be removed after completion of each carbonization cycle, for example by means of a slide from the tub 13 and fed to a further treatment or disposal. To the trough 13, a Trübkondensatentnahmeleitung 22 leading out of the autoclave 1 is connected, through which, if desired, turbidity condensate 18 during a carbonation cycle from the trough 13 and thus then also from the autoclave 1 can be derived. On the other hand, however, this cloudy condensate removal line 22 can also be used as a feed line for introducing process water into the trough 13 at the beginning or before a carbonization cycle so that it can evaporate before the turbidity condensate 18 is obtained during the carbonation cycle.

Furthermore, the autoclave 1 a Klarkondensatentnahmeleitung 23, by means of which the Klarkondensathsammelraum 21 contaminated Klarkondensat 7 can be removed, which can then be disposed of in a municipal sewage treatment plant.

In order to be able to discharge air from the autoclave-side reaction space 2, if desired, the autoclave 1 also has a vent 20.

As can be seen from FIG. 4, an autoclave 1 can be part of a system 24 which comprises a plurality of autoclaves 1, 25, 26 or one or more heat accumulators 27. Here, the various units are interconnected in parallel and connected to each other via a steam shuttle 28, wherein in each case a steam line 29 branches off from the steam shuttle 28 and opens into the respective autoclave 1, 25, 26 or a respective heat storage 27. In order to make the necessary for the complete achievement of the biomass 4 for carrying out the hydrothermal carbonization reaction steam penetration into the biomass 4, steam guide tubes 30 are arranged in the container 16, in which the water vapor generated in the autoclave inside the reaction chamber 2 free from both ends of a each steam guide tube 30 flow into this and then can flow through the perforated wall of each steam guide tube 30 into which the respective steam guide tube 30 surrounding biomass 4. The autoclaves 1, 25 and 26 interconnected or interacting in the plant 24 are autoclaves of at least substantially the same design, all of which have the same design as the autoclave 1 illustrated in connection with FIG. 2 and explained above. The water vapor generating unit 11 with the trough 13 extends substantially along most of the longitudinal extent of the autoclave 1 and is formed in this longitudinal direction at least as long as the container 16 containing the biomass 4. In the same way, the heat energy coupling part 12 extends in the longitudinal direction of the autoclave 1, wherein the trough 13 only by a front, beveled inclined end

31 over the heat energy coupling part 12 projects, as shown in FIG. 3 can be seen. With this embodiment, the heat exchanger 3 then also has a longitudinal extension which corresponds approximately to, preferably at least, the longitudinal extension of the container 16 in the longitudinal direction of the autoclave 1 and also covers the essential part of the longitudinal extension of the autoclave 1. The inclined part 31 forms the front, the opening door or opening flap of the autoclave 1 associated side of the heat exchanger 3 and the trough 13 from. The container 16 is shown in the embodiment as designed with predominantly perforated or lattice-structured side walls container 16. But it is quite possible that formed as baffles 17 wall portions are formed not only in the lower third, but over the entire side surfaces of the container 16, so that he only one perforated top, or even a completely open top, and a perforated underside that prevents biocleamage from falling through.

With the autoclave 1 or the system 24 according to the invention, both a so-called cold start for initiating or initiating a hydrothermal carbonization cycle and a so-called warm start can be carried out. In the case of a cold start, no water vapor is supplied from the outside to the autoclave-side reaction space 2. However, if the autoclave 1 is, for example, part of a multiple autoclave 1, 25, 26 and / or a heat storage 27 comprehensive system 24, but may also be a warm start of the autoclave 1 by means of the outside via the steam shuttle 28 of a further autoclave 25, 26th or the heat storage 27 supplied steam are performed. In the case of a cold start, all autoclaves 1, 25 and 26 are initially out of operation in a system 24 and the at least one heat accumulator 27 is not charged. Thus, steam must first be generated within one of the autoclaves 1, 25, 26 with the aid of the external steam generator 8 and the steam / condensate circuit 9 for the first time. This should be the autoclave 1. In such a cold start, the trough 13 of the Wasserdampferzeugungseinhelt 1 1 of the autoclave 1 with liquid, especially water, filled. The autoclave 1 is then loaded with the biomass 4 by positioning the container 16 containing the biomass 4 in the position shown in FIG. 2 in the autoclave 1 and in the autoclave-side reaction space 2. Thereafter, the door, not shown, of the autoclave 1 is closed and locked, so that the autoclave 1 is closed pressure-resistant. In the next step, the heat energy coupling part 12 of the heat exchanger or heat exchanger 3 is acted upon by steam of the steam / condensate circuit 9 of the external steam generator 8. The supplied water vapor gives off most of its heat energy in the heat energy coupling part 12 and condenses into a clean condensate, which is returned to the external steam generator 8. Due to the heating of the heat energy coupling part 12 of the heat exchanger 3, heat energy is coupled into the heat exchanger 3, and indeed by the heat energy coupling part 12 in the Wasserdampferzeugungseinhelt 1 1, and registered. Thereby begins the existing in the tub 13 liquid at cold start in particular supplied water (process water) or existing reaction water or turbidity condensate 18, evaporate or vaporize. The autoclave 1 is then vented by means of the vent 20. After the vent 20 is closed again, then with further energy input through the steam / condensate circuit 9, the further evaporation of the reaction water located in the tub 13 or Trübkondensats 18 and, consequently, a temperature of the autoclave inside reaction chamber 2 and a pressure buildup in the autoclave inside reaction chamber. 2 by the resulting water vapor. By regulating the heating of the heat energy coupling part 12 of the heat exchanger 3, ie the regulation of the supply of steam in the steam / condensate circuit 9, the vapor pressure in the autoclave inside reaction chamber 2 is controlled and adjusted. The water-containing component contained in the water vapor flows through the biomass, here starts the hydrothermal carbonation reaction and condenses in the biomass 4, but also on the container 16 and on the inside of the container 10. From the container 16 and the biomass 4, this condensate occurs as water of reaction or turbidity condensate 18 and is then collected in the formed by the tub 13 Trübkondensatsraumel 19. Another, outside of the container 16, in particular on the inside of the container

Autoclave wall 10 condensing part of the water vapor condenses here as a contaminated Clarkondensat 7, which collects in the deepest region of the autoclave 1 in the formed there Klarkondensathsammelraum 21. Depending on the composition of the biomass 4 exposed to the hydrothermal carbonization process, turbidity condensate 18 can either be withdrawn from the trough 13 via the turbidity condensate removal line 22 or process water can be supplied to the trough 13. This happens depending on which steam atmosphere is to be set in the autoclave inside reaction space 2 and whether the water required for this is present sufficiently or in excess. Is too much water, in particular

Turbidity condensate 18, is present, turbidity condensate 18 is removed. If too little water is contained in the biomass 4 and too little turbidity condensate 18 forms, then process water is supplied from the outside. The collecting in the bottom region of the autoclave 1 Klarkondensat 7 is continuously from the autoclave inside reaction space 2 and thus derived and discharged to the autoclave 1. Depending on the biomass 4 to be carbonized, the desired and necessary water vapor pressure, the desired and necessary steam temperature and the desired and necessary holding time are set in the autoclave 1 or in the autoclave inside reaction space 2. As soon as the steam pressure has reached its setpoint value in the autoclave-side reaction space 2, further water vapor which has formed can be released via the steam line 29 to the connected steam displacement line 28. Via the vapor displacement line 28, this vapor can then be fed to one or both of the adjacent autoclaves 25 and 26 and / or the heat accumulator 27. After the holding time, the water vapor pressure in the autoclave 1 is then reduced. This can be done or supported, that in turn steam is delivered to the steam shuttle line 28. Incidentally, the water vapor pressure is controlled by corresponding reduction of the heating of the heat energy coupling part 12. In this case, the heating can then also be regulated so that, if desired, the entire turbidity condensate 18 is vaporized at the end of a carbonization cycle and in the tub 13 only the sewage sludge 6 is located. After then, finally, the heating of the evaporator 31 and the heat exchanger 3 is turned off and the pressure in

Autoclave 1 is reduced to atmospheric pressure, the autoclave 1 is opened and the cage or container 16 with the now hydrothermally biochar 5 carbonized biomass 4 taken from the autoclave 1. It can then be decided whether the sewage sludge 6 present in the tank 13 is removed or if necessary still remaining in the tank 13 for a next carbonization cycle.

A warm start is performed when at least one of the autoclaves 1, 25 and 26 is already in operation, i.e. in the plant shown in FIG. is in an ongoing carbonization cycle, and / or a loading

Heat storage 27 is available. In such a warm start can then be placed in a carbonization cycle autoclave, here now the autoclave 1, both of the external steam generator 8 by means of the autoclave inside the reaction chamber 2 integrated evaporator 31 and Heat exchanger 3 are heated and are acted upon by one of the adjacent autoclave 25, 26 or the heat storage 27 via the steam shuttle line 28 and the steam line 29 directly and directly with steam. The use of the various heat sources for the generation or supply of water vapor can be flexibly handled and used here. The use is determined by the type and amount of turbidity condensate 18 in the tub 13, the composition of the biomass 4 and the thermal state of the system 24, ie the steam potential available within installation 24.

When a warm start can be in the tub 13 as in the cold start cloudy condensate 8, there process water can be entered or may be in contrast to the tub 13 initially completely dry. Even during the warm start of the autoclave 1 is then initially loaded with biomass 4 and the door of the autoclave is closed and locked. The autoclave 1 to be started, which is considered here, is then operated via the vapor displacement line 28, which is already in operation in this embodiment, i. in a carbonization cycle, located autoclave 25, 26 or the heat storage 27 supplied with water vapor. The autoclave 1 is vented and after closing the vent 20 then begins the pressure build-up in the autoclave inside

Reaction space 2 by means of the still supplied from one of the autoclave 25, 26 or the heat storage 27 steam. As with the cold start, part of the water vapor condenses due to heat release to the biomass 4, the biomass container 6 or the inside of the autoclave wall 10 and is collected as cloudy condensate 18 or water of reaction in the tub 13 or as contaminated clear condensate 7 in the bottom region of the autoclave 1. As with the cold start, it is now possible, depending on the composition of the biomass 4, to remove turbid condensate from the trough 13 via the turbidity condensate removal line 22 or to introduce liquid into the trough 13. The contaminated clear condensate 7 obtained in the bottom region of the autoclave 1 is preferably removed from the autoclave 1 continuously via the clear condensate removal line 23. After a certain time, then the supply of water vapor from an adjacent autoclave 25, 26 and / or the heat storage 27 is set, since there is no corresponding water vapor more is available, and the necessary for the generation of steam heat input via the supply of steam from the external steam generator 8 in the heat exchanger 3. Again, then runs the steam / condensate circuit 9 through the heat energy coupling part 12 and causes the energy input in the steam generating unit 11. As with the cold start is by the heating of the integrated heat exchanger

3 now the liquid contained in the tub 13, i. the turbidity condensate 18, evaporates and become dependent on the composition of the biomass

4, the water vapor pressure, the steam temperature and the holding time in the autoclave 1 are set and regulated. The warm start now runs like the cold start.

After reaching the desired setpoint pressure, steam can be delivered to the vapor displacement line 28 and adjacent autoclaves 25, 26 or the heat accumulator 27, and after the desired holding time has elapsed, the pressure is reduced in an analogous manner to the cold start in the autoclave inside reaction space 2. When the autoclave-side reaction space 2 is then at atmospheric pressure, the autoclave 1 can be opened and the biomass 4 carbonated to biochar 5 or green goal or biochar can be removed. It can be seen from the above that the cold start and the warm start differ only in how the required water vapor is provided at the beginning of a carbonization cycle. During the cold start, this autoclave 1 is completely produced within the one carbonation cycle, whereas the steam is initially provided and supplied by a previously identical autoclave 25, 26 or a heat accumulator 27 in the case of a warm start initially, and thus partially over the entire carbonization cycle becomes.

In one of the three autoclaves 1, 25, 26, the heat storage 27 and the steam return line 28 with connected steam lines 29 include

Appendix 24, such a warm start, for example, be carried out according to the following embodiment. It is here that the autoclave 1 is to be started, the autoclave 25 is in the middle of its carbonization cycle and the autoclave 26 at the end of his Carbonization cycle is located. The autoclave 1 is depressurized at the beginning of the warm start and thus at the beginning of the carbonization cycle, the autoclave 25 has in its autoclave inside reaction chamber 2 a steam atmosphere of 16 bar and 200 ° C, the autoclave 26 has in its autoclave inside reaction chamber 2 a water vapor atmosphere of 16 bar and 200 ° C and the heat storage 27 provides water vapor at a pressure of 4 bar and a temperature of 145 ° C available.

In such a Ausführungsbeispiei then the tub 13 of the autoclave 1 is left dry or filled with liquid depending on the composition of the biomass 4 and the autoclave 1 is loaded with the biomass 4. Thereafter, the door of the autoclave 1 is closed and locked. The now beginning with the steaming of the biomass 4 comprehensive part of the carbonization cycle beginning Kohleisierungszyklusabschnitt by the autoclave 1 from the heat storage 27 steam at 4 bar and 145 ° C is fed. The autoclave 1 is then vented again (duration about 10 min). After closing the vent 20, the pressure build-up in the autoclave inside reaction chamber 2 to 3 bar (duration about 10 min) by further water vapor at 4 bar and 145 ° C from the heat storage 27 is supplied. Subsequently, the autoclave 1 is then supplied with steam from the autoclave 26 at the end of its cycle, the water vapor pressure in the autoclave 26 being reduced from 16 bar to 8 bar. The water vapor pressure in the autoclave 1 increases from 3 bar to 7 bar (duration about 10 min). Thereafter, the autoclave 1 is then supplied with 16 bar of water vapor from the autoclave 25. The water vapor pressure in the autoclave inside

Reaction space 2 of the autoclave 1 is increased within 20 minutes from 7 bar to about 16 bar and then adjusted to 16 bar water vapor pressure (duration about 120 min). As already described above in connection with the cold and warm start, condenses a part of the water vapor by heat to the biomass 4, the biomass container 16 or the

Autoclave 10 and falls on the one hand as turbidity condensate 18 in the tub 13 or as a contaminated Clarkondensat 7 in Klarkondensathsammelraum 21 in the bottom region of the autoclave 1 at. Depending on the composition of the biomass 4 reaction water or turbidity condensate 18 from the tub 13th be removed and discharged or fed or supplied to this process water. The clear condensate 7 is continuously discharged from the autoclave 1. After the autoclave 1 has been supplied for about 120 minutes with steam from the autoclave 26, then the integrated water vapor generating unit 1 1 of the heat exchanger 3 in the autoclave 1 by supplying steam from the external steam generator 8 - as in connection with the cold and Warm start described - set in motion. By heating the integrated heat exchanger 3, the liquid begins to evaporate in the tub 13 and the autoclave 1 can now during this period of the carbonization cycle of about 240 min steam with a pressure of 16 bar to the steam shuttle line 28. After expiration of the holding time in autoclave 1 of about 360 min, the water vapor pressure, ie the pressure in the autoclave 1 gradually over the stages 8 bar and 5 bar reduced to 1 bar (duration in each case about 10 min). In this case, steam can be delivered to one of the adjacent autoclaves 25, 26 and / or the heat accumulator 27. The heating of the internal evaporator 31 or heat exchanger 3 is then in turn adapted to the desired evaporation of the turbidity condensate 18 and carried out according to the specific requirements of its evaporation. Finally, the heating of the internal heat exchanger 3 is turned off and the pressure in the autoclave 1 is reduced to atmospheric pressure, so that the autoclave 1 is opened and the reaction product, the biomass 4 carbonated to green coal or biochar 5 or biochar biomass 4, together with the surrounding container 16, the Autoclave 1 can be removed. In the embodiment finds an autoclave 1 with a length of 12 m and a

Inner diameter of 1, 8 m use. In these plants, 7.5 t of biomass 4 are converted to biochar 5 in a hydrothermal carbonation cycle as part of a carbonation reaction. For this cycle, about 4 tons of steam are needed. The hydrothermal carbonization cycle has a length of about 480 min and comprises the following steps:

Loading the autoclave 1 with biomass: approx. 20 min

Pressure build-up in the autoclave to 16 bar: approx. 50 min

Holding time in autoclave 1 at 16 bar: approx. 360 min Pressure reduction in an autoclave to 1 bar: approx. 30 min

Discharging the generated biochar: approx. 20 min

With the method described above and the autoclave 1 described above, coal 5, so-called biochar or biochar or green coal can thus be produced in the course of a batch-wise batch production from biomass 4 by means of hydrothermal carbonization. The generated and used steam is predominantly and preferably saturated steam.

Due to the fact that the clear condensate 7 formed by condensation on the inside of the autoclave wall 10 is collected separately from the reaction water leaving the biomass 4 (steam condensate + split-off organic water), the turbid condensate 18, it is found in which, after adequate dilution of the Trübkondensats 18 in the tub 13 forming sewage sludge 6 salts and ash formers such as sodium and potassium chlorides, so that the sewage sludge 6 has a pH of 3-4.

Although the exemplary embodiment above merely comprises a container 16 for receiving the biomass 4, it is also possible for a plurality of containers 6 to be arranged adjacent to one another over the longitudinal extent of the autoclave 1 above the trough 13.

The carbonization process or the actual carbonization reaction is carried out with steam in the temperature range from 160 ° C to 370 ° C, preferably to 370 ° C, and 10 bar - 60 bar.

The sewage sludge 6 can be further processed for the recovery of the components therein, for example for the production of phosphorus.

In order to specifically condense on the inside of the autoclave wall 10 Klarkondensat 7, it may also be provided to cool the autoclave wall 10, for example by means disposed in the autoclave wall 10, water-carrying cooling tubes. In the embodiment, an external steam generator 8 is provided with connected steam / condensate circuit 9, which supplies the tubes 14 and thus the heat energy coupling part 12 steam. However, alternative embodiments are also conceivable in which, instead of steam, the tubes 14 are supplied with another heat transfer fluid, for example a heat transfer oil circulating in a solar thermal system.

Furthermore, in the context of the present invention, the term "coal" 5 produced in the context of the carbonization process also means peat-like material, because depending on the conditions (pressure, temperature, holding time etc.) under which the carbonization process is carried out in each case, the obtained converted biomass of peat-like / peat-like to carbonaceous / coal-like.

Even if the embodiment for the befindlicher for the evaporation of liquid in the tub 13, such as water, process water, water of reaction or turbid condensate 18, required heat energy and thus required for the steam generation in the autoclave inside reaction chamber 2 heat energy at least partially by means of the tubes 14 of the evaporator. 3 supplied external water vapor or a heat transfer fluid, it is also within the scope of the invention, the heat exchanger 3 and / or the water vapor generating unit 11 and / or the heat energy coupling part 12 and / or the evaporator 31 as an electrically heated device, for example by means of built-in heating wires form.

Claims

claims

1. A process for the production of coal (5) from biomass (4) by means of hydrothermal carbonation in an autoclave (1), the autoclave inside reaction space at the beginning of each of the conversion of the biomass (4) in coal (5) comprehensive carbonization cycle to be carbonated with carbonated Biomass (4) is filled, wherein the carbonization reaction of the biomass (4) in the autoclave (1) carried out in an at least predominantly steam atmosphere and the carbonization is effected by means of in the biomass (4) initiated water vapor pressure, characterized

in that the steam of the biomass (4) causing water pressure of increased pressure during the respective carbonization cycle at least temporarily in the autoclave inside reaction space (2) of the autoclave (1) filled with the biomass (4) to be carbonized by means of at least one evaporator (31 ) is produced.

2. The method according to claim 1, characterized in that the carbonization of the biomass (4) causing water pressure increased pressure during the respective carbonization cycle at least for a period of at least 30% of the time of a carbonization cycle, during which steam increased pressure in the autoclave inside reaction space (2) is required for the course of the carbonation reaction is generated by means of at least one evaporator (31) arranged therein.

3. The method according to claim 1 or 2, characterized in that the carbonization of the biomass (4) causing water vapor increased pressure during the respective carbonization cycle substantially and / or predominantly in the with the biomass to be carbonized (4) filled autoclave inside reaction space (2 ) of the autoclave (1) is produced by means of the at least one evaporator (31) formed and arranged therein.

4. The method according to any one of the preceding claims, characterized in that in the autoclave inside reaction space (2) of the autoclave (1) generated by means of a steam in the autoclave inside the reaction chamber (2) of the autoclave (1) arranged heat exchanger (3) with associated, in particular integrated, and in the autoclave inside the reaction chamber (2) of the autoclave (1) arranged water vapor generating unit (11) is generated.

5. The method according to any one of the preceding claims, characterized in that during the carbonization cycle from the biomass (4) leaking liquid is fed to a in the autoclave inside reaction space (2) formed Trübkondensatsammelraum (19) and / or on the inner wall regions of the autoclave inside reaction space (2) Convective condensate is fed to a in the autoclave inside the reaction chamber (2) formed Klarkondensathammelraum (21).

6. The method according to any one of the preceding claims, characterized in that a part of the carbonization of the biomass (4) causing water pressure increased pressure during each in the autoclave inside reaction space (2) running carbonization cycle, in particular at the beginning of the carbonization cycle, the autoclave inside reaction space (2 ) is supplied from one or more autoclaves (25, 26) of the same type connected in parallel and / or that a part of the water vapor of the increased carbonization of the biomass (4) causes the autoclave interior reaction space (see FIG. 2) of a parallel-connected autoclave (25, 26) of the same type is supplied.

7. The method according to any one of the preceding claims, characterized in that a part of the carbonization of the biomass (4) causing water pressure increased pressure during the respective in the autoclave inside reaction space (2) running carbonization cycle, in particular at the beginning of the carbonization cycle, the autoclave inside reaction space (2 ) is supplied from a heat storage (27) and / or that a part of the carbonization of the biomass (4) causing water pressure increased during the respective in the autoclave inside reaction space (2) running carbonization cycle from the autoclave inside reaction space (2) a heat storage (27) is supplied.

8. The method according to any one of the preceding claims, characterized in that the autoclave inside reaction space (2) at the beginning of each conversion of the biomass (4) in coal (5) comprehensive carbonization cycle is not or only partially and partially filled with water of reaction to be evaporated ,

9. autoclave (1) for generating coal (5) from biomass (4) by means of hydrothermal carbonation in an at least predominantly steam-shaped medium, in particular for carrying out a method according to any one of claims 1-8, the autoclave inside reaction space (2) for carrying out the hydrothermal carbonization partly with reaction and / or process water and batchwise with biomass to be carbonated (4) can be filled, and in which the carbonization reaction of the biomass (4) in an at least predominantly steam atmosphere and by means of the biomass (4) initiated steam increased pressure is feasible, and the one, the biomass to be carbonated (4) and during a carbonization cycle in the autoclave (1) positioned container (16), characterized in that the autoclave inside reaction space (2) has an evaporator (31).

10. autoclave (1) according to claim 9, characterized in that the evaporator (31) has a heat exchanger (3) with associated, in particular integrated, and in the autoclave inside reaction space

(2) arranged water vapor generating unit (1 1) comprises, in particular designed as such.

1 autoclave (1) according to claim 9 or 10, characterized in that the heat exchanger (3) decouples heat energy supplied to the water vapor generating unit (1 1).

12. autoclave (1) according to any one of claims 9 to 1 1, characterized in that the heat exchanger (3) through which a heat transfer fluid can flow, preferably wasserdampfdurchströmbare, tubes (14) and heat energy to the water vapor generating unit (1 1) auskoppelnden heat energy coupling part ( 12) which is in heat-conducting connection with the steam generator unit (1 1).

13. autoclave (1) according to one of claims 9 to 12, characterized in that the water vapor generating unit (1 1) as in the heat exchanger

(3) and its heat energy coupling part (12) integrated and upper side on the heat energy coupling part (12) in the form of, in particular vvao ci i iaiuyc,

i iailcnuci i tub 'auaycunucic i_ II II ICI L is formed.

14. autoclave (1) according to one of claims 9 to 13, characterized in that the water vapor generating unit (1 1) of the heat exchanger (3), preferably the heat energy coupling part (12) and the water vapor generating unit (1 1) of the heat exchanger s (3), in the autoclave inside reaction space (2) below the container to be carbonized (4) receiving container (16) and with Distance to the autoclave inside bottom surface of the reaction chamber (2) are arranged.

15. autoclave (1) according to any one of claims 9 to 14, characterized in that the water vapor generating unit (11) are associated with means (17), which supply her during the carbonization cycle from the biomass (4) exiting reaction water or turbidity condensate (18) or forward.

16. autoclave (1) according to claim 14 and 15, characterized in that the water vapor generating unit () associated with means as wall portions of the container (16) forming and liquid on the liquid receiving and / or holding portion of the trough (13) supplying baffles ( 17) are formed.

17. autoclave (1) according to one of claims 9 to 16, characterized in that the water vapor generating unit (11), in particular of the liquid receiving and / or holding portion of the trough (13), from the biomass (4) leaking fluid, in particular reaction water and / or turbidity condensate (18), receiving turbidity condensate collecting space (19) is formed.

18. autoclave (1) according to one of claims 9 to 17, characterized in that in the wall region of the autoclave inside reaction space (2), in particular below the evaporator (31), preferably below the steam generator unit (11) of the heat exchanger (3), in particular below the trough (13), particularly preferably below the heat energy coupling part (12), a condensate collecting condensate (21) condensing and draining off on the inner wall regions of the autoclave inside reaction chamber (2) is formed. Autoclave (1) according to claim 17 or 18, characterized in that the turbidity condensate collecting space (19) leading out of the autoclave (1) Trübkondensatentnahmeleitung (22) and / or the Klarkondensathammelraum (21) from the autoclave (1) leading out Klarkondensatentnahmeleitung (23 ).

Autoclave (1) according to any one of claims 9 to 19, characterized in that the evaporator (31), in particular the heat energy coupling part (12) and the water vapor generating unit (1 1) of the heat exchanger (3), are designed such that so that for the batchwise carrying out a carbonization cycle of the introduced with the container (16) biomass (4) in the autoclave interior reaction chamber (2) required amount of steam at least substantially, preferably predominantly, if desired completely, in the autoclave inside reaction space (2) can be generated.

Autoclave (1) according to one of claims 9 to 20, characterized in that it is connected to a vapor recovery line (28) via which its autoclave inside reaction space (2) with the autoclave inside reaction space (2) at least one second autoclave (25, 26) of the same type and / or a heat storage (27) is connected.

Autoclave (1) according to any one of claims 9 to 21, characterized in that in the container (16) a plurality of extending therethrough and at least one end, preferably both ends, accessible for incoming water vapor and perforated in its tube wall steam guide tubes (30) are formed.

Plant (1) for producing coal (5) from biomass (4) by means of hydrothermal carbonization in an at least predominantly steam-shaped medium, in particular for carrying out a method according to one of claims 1 to 8, characterized in that they have a plurality of autoclaves (1, 25, 26) with their respective autoclave-side reaction spaces (2) in steam-conducting line connection (28, 29) according to one or more of claims 9-22, one or more with at least the autoclave-side reaction space (2 ) one of the autoclaves (1, 25,

26) in steam-conducting line connection (28, 29) standing (n) heat storage (27) and one or more with a steam generating unit (11), in particular the heat energy coupling part (12), a autoclave inside heat exchanger s (3) at least one of the autoclave (1 .

25, 26) in steam-conducting line connection standing (s) steam generator (8).