CH706162A2 - Carbonation tank for hydrothermal carbonizing a highly viscous and/or particulate-loaded process medium, comprises carbonation tank hollow volume enclosed by carbonation tank sheath, heat transfer channel extending from inlet to outlet - Google Patents

Abstract

Carbonation tank (11) comprises a carbonation tank hollow volume for hydrothermal carbonizing a highly viscous and/or particulate-loaded process medium (5). The hollow volume is enclosed by a carbonation tank sheath (110) that is storable in a fluid (3). A heat transfer channel (116) is arranged completely traversing the carbonizing tank, which extends from an inlet to an outlet. The interior of the heat transfer channel is completely separable from the filled process medium by walls of the heat transfer channel, and the fluid is flowable from the interior of the heat transfer channel. Carbonation tank (11) comprises a carbonation tank hollow volume for hydrothermal carbonizing a highly viscous and/or particulate-loaded process medium (5). The hollow volume is enclosed by a carbonation tank sheath (110) that is storable in a fluid (3), where the process medium and the fluid are separated from each other. A heat transfer channel (116) is arranged completely traversing the carbonizing tank, which extends from an inlet to an outlet. The interior of the heat transfer channel is completely separable from the filled process medium by walls of the heat transfer channel, and the fluid is flowable from the interior of the heat transfer channel. Independent claims are also included for: (1) a reactor comprising the above mentioned carbonization tank with the completely traversing heat transfer channel, and an outer container, where the carbonization tank is positionable within the outer container, which is surrounded by the fluid, and a pressurizing unit is designed by a hydraulic pressure of the fluid for specifically adjusting the variation of the carbonization tank hollow volume from outside the carbonization tank during carbonization process; (2) a pressure-tight carbonization tank for carrying out hydrothermal carbonization, stirring and introducing the high viscosity and/or particulate-loaded process medium, comprising the carbonation tank sheath including the carbonization tank hollow volume, where at least one portion of the carbonization tank sheath has a multipart design, in which the parts are arranged separated from each other in a pressure- and liquid-tight manner and are movably mounted relative to each other defining reproducibility such that the carbonization tank hollow volume is specifically changeable and the internal pressure of the process medium in the carbonization tank is adjustable irrespective of the process temperature; (3) a use of the pressure-tight carbonization tank for hydrothermal carbonization of the filled process medium, where the volumetric capacity of carbonization tank is adaptable based on the amount of the filled process medium, and the internal pressure in the carbonization tank is adjustable irrespective of the temperature of the process medium and the water vapor saturation curve from the outside of the carbonization tank; and (4) a hydrothermal carbonization system including the multipart reactor, comprising the above mentioned carbonization tank, which is mounted in the outer container, where the carbonization tank hollow volume of the carbonization tank is specifically changeable and the internal pressure of the process medium that is independent of the process temperature is achievable in the carbonization tank.

Description

Technical area

The present invention describes a Karbonisierungsbehälter comprising, enclosed by a Karbonisierungsbehältermantel carbonization container volume for the hydrothermal carbonation of a highly viscous and / or solids-laden process medium, the Karbonisierungsbehältermantel in a fluid, completed by the process medium, is storable and a reactor comprising a Karbonisierungsbehälter with a heat transfer channel.

State of the art

Under hydrothermal carbonization (HTC) or wet charring is understood to mean the refining of wet or moist biomass in aqueous mostly acidic environment at elevated temperatures by 200 ° C and elevated pressures of more than 10 bar in a pressure-tight Karbonisierungsbehälter. In order to start the hydrothermal carbonization, the biomass, water and catalytically active substances must first be heated to the elevated temperature at the beginning. Subsequently, the reactants react to intermediates and ultimately to Karbonisierungsprodukten, which are in the form of a biochar or brown coal suspension, which contains not only coal but also process water and residual substances. By hydrothermal carbonation, the natural process of coal formation is technically reproduced within a few hours and above all the high carbon efficiency distinguishes the HTC.

In the present application is understood as a fermentable biomass and thus as part of the starting materials, which can be processed by the hydrothermal carbonization to coal, preferably a mixture of sewage sludge and green waste. In the described reactor, however, other biogenic residues, in particular renewable raw materials, such as wood chips, green cuttings from landscape care, plants, straw, silage, and organic residues from agriculture and forestry and the food industry and waste management, as well as peat, lignite, Paper sludge, to be refined into masses with a high proportion of coal.

Since the described reaction of a highly viscous and / or solid-laden process medium of a biomass added liquid and thus a solid-liquid mixture in reaction times of a few hours under high pressure and elevated temperatures, specially adapted reactors and stirring and conveying devices are required ,

To arrange the Karbonisierungsbehälter in an outer container, wherein the outer container is filled with a thermal fluid, in particular thermal oil, is known for example from DE102 010 020 712. By contact with the thermal oil, the process medium can be heated within the Karbonisierungsbehälters from the beginning of the reaction to the required temperatures of about 200 ° C.

According to DE10 2010 020 712, the carbonating container projects at least partially into the outer container and the thermal oil located therein. Thermal energy can be transferred to the thermal oil as soon as the exothermic reaction of charring occurs, thus protecting the carbonator from overheating. To reduce the reaction time, the contents are preheated with a second heat exchanger. In DE10 2010 020 712, the exhaust gases of a combined heat and power plant serve as heat energy source for the heating of the thermal oil. This energy is inexpensive and basically as a waste product due to the high exhaust gas temperatures of about 400 ° C sufficient for heating the thermal oil to up to 250 ° C before. Due to the abundance can be dispensed with a most efficient embodiment of the heat transfer. If the possibility of heat transfer were optimized, even more consumers could benefit from the excess heat of the combined heat and power plant.

In WO 2008 095 589 an improved heat transfer is achieved by providing a heat exchanger in the form of an outer container filled with thermal oil, wherein a arranged in the outer container Karbonisierungsbehälter is designed in the form of a bent pipe. Depending on the embodiment, the Karbonisierungsbehälter may have a different number of approximately U-shaped bends. The multi-curved carbonation container in tube form is completely surrounded by thermal oil and passed through the outer container from an inlet to an outlet. Due to the enlarged surface of the bent and in comparison to the outer container thinly designed carbonation container, the walls of the carbonation container are extensively in contact with the thermal oil, so that thermal energy is optimally transferable.

The achievable with these means possibilities of heat exchange from the process medium through the walls of the Karbonisierungsbehälters on the thermal oil and back are indeed improved, however, special curved Karbonisierungsbehälter must be made, their production costly and its construction and operation are complicated.

Due to the transport of the solid-liquid mixture comprising biomass and an aqueous solution, resulting in a solid-laden liquid, the use of a low-profile pipeline and the curved configuration of the Karbonisierungsbehälters leads to a reduced throughput. The bent pipe is accordingly prone to clogging. Since the temperature of the process medium increases in the course of the reaction and reaches a maximum in the vicinity of the outlet, that is, has a temperature gradient, the bent configuration of the carbonization container is subjected to varying degrees of thermal stress so that the carbonization container is susceptible to wear.

When using a bent pipe, the use of an agitator for feeding and distribution of the process medium in the direction of outlet is only possible with difficulty. Such agitators would have to be isolated or bent in different sections in order to ensure a feed.

It can not be ruled out that there are blockages and occur due to the strongly heated process medium selectively strong thermal and mechanical stresses on the wall of Karbonisierungsbehälters.

Presentation of the invention

The present invention has for its object to provide a Karbonisierungsbehälter, which allows improved heat transfer from the process medium through the walls of the Karbonisierungsbehälters on the fluid with simplified production, whereby an energy-efficient hydrothermal carbonization can be achieved.

Another object of the invention is to avoid bent pipes which are heated to different degrees, since the formation of a temperature gradient is reduced. As a result, the creation of low-wear Karbonisierungsbehälter is possible.

This object is achieved by a carbonation vessel which has a heat transfer channel which traverses the carbonation vessel and allows complete circulation of the thermal oil around the carbonation vessel and through the heat transfer channel. The heat transfer channel carries the thermal fluid and is otherwise separated from the interior of the Karbonisierungsbehälters and thus by the process medium through walls.

To solve the problem, the Karbonisierungsbehälter is equipped for example with a concentric to the longitudinal axis extending heat transfer channel, which completely crosses the Karbonisierungsbehälter. The area of the inner surfaces coming into contact with the process medium, as well as the outer surfaces of the carbonization container coming into contact with thermal oil, are greatly increased and better heat transfer from the process medium to the thermal oil can be achieved.

Brief description of the drawings

A preferred embodiment of the subject invention will be described below in conjunction with the accompanying drawings. <Tb> FIG. 1a shows a perspective view of an outer container of a reactor, which is mounted on a reactor storage device and is coupled to an input and output device, during <Tb> FIG. 1b shows a side view of the outer container with a view of the base bottom. <Tb> FIG. FIG. 2 shows a perspective view of a reactor with attached feed and discharge device, wherein the reactor storage device has been omitted, while FIG <Tb> FIG. Figure 3 shows a side view of the reactor of Figure 2. <Tb> FIG. 4 shows a horizontal section through the reactor according to line C-C from FIG. 3, wherein the process container in the interior of the outer container becomes clear. <Tb> FIG. 5a shows a vertical section of the reactor according to FIG. 1a, the process medium in the carbonization container and the thermal oil in the outer container being shown, for better clarity, but the supply and removal device has been omitted, and FIG <Tb> FIG. 5b <sep> shows a section in a perspective view through the reactor according to FIG. 5a, without process medium and thermal oil.

description

The present application describes a hydrothermal Karbonisierungsanlage, comprising a multi-part reactor 1 in which the hydrothermal carbonization of a highly viscous and / or solid-laden process medium can be carried out efficiently and continuously. The highly viscous and / or solid-laden process medium comprises filling material which consists of raw biomass of various composition and consistency, process water and additives, e.g. Catalysts exists. Due to its composition, the process medium is present as a suspension or as sludge, with liquid fractions being mixed with solids. The content of contents of the process medium is also considered to be a starting material, since it forms a solid-liquid mixture which is converted in the course of the hydrothermal carbonation into carbonization products comprising charred biomass. The carbonation products form a charred portion of the process medium, which has a similar solid-liquid consistency to the starting materials, with the solid components being at best fully converted to brown coal.

The starting materials are introduced into the reactor 1 of the Karbonisierungsanlage, under high pressure and elevated temperature, as known from the basics of hydrothermal carbonization, charred after the process as Karbonisierungsprodukte discharged from the reactor 1. The introduction and removal or the supply and discharge of educts and Karbonisierungsprodukte can take place in portions during operation of the Karbonisierungsverfahrens, the Karbonisierungsprozess is not significantly disturbed and is not interrupted and thus can proceed quasi-continuously.

The reactor 1 comprises an outer container 10, which is rigid and serves as a pressure vessel. The outer container 10 is rotatably mounted on a reactor storage device 2 about the outer container longitudinal axis La. On two racks 20 pivot bearings 21 are arranged so that the outer container 10 is controlled by at least one rotary drive 22 rotatable. As a rotary drive 22, for example, suitably dimensioned electric motors. This rotatable storage of the reactor 1 is used to support the Karbonisierungsprozesses, but is not mandatory.

In the embodiment shown here, the outer container 10 has an outer container shell 100 with a cylindrical centerpiece 1003, which is closed off by a base base 1001 by a base flange 1002 releasably lockable and liquid-tight and pressure-tight. From the base bottom 1001 side, the process medium is supplied and discharged. On the base bottom 1001 opposite side of the outer container shell 100, the cylindrical centerpiece 1003 is closed by a curved lid bottom 1005 executed by means of Deckelbodenflansch 1004 releasably liquid and pressure-tight. The outer container 10 is stored lying, wherein the outer container longitudinal axis La extends approximately horizontally to the level of the ground at the site. The outer container 10 is detachably closable and thus completed the process of hydrothermal carbonization through the outer container 10 in the reactor 1 from the environment.

The outer container 10 is rigid for stability reasons and preferably made of steel, wherein the wall thicknesses are chosen so that even fluid pressures of several bar can be safely formed within the outer container 10, which the outer container 10 can withstand. Depending on the planned plant size and the amount of educts to be converted, the size of the outer container interior 103 is selected.

In the base bottom 1001 a filling passage 104 and an output passage 105 is arranged completely crossing, whereby access to the outer container 10 from the outside is possible with otherwise closed outer container 10. In Fig. 1b, a stirrer drive means 132 is shown, which will be explained in connection with a stirring and conveying device.

Fig. 2 shows a reactor 1 with a possible embodiment of a connected feed and discharge device 4. On the reactor storage device 2 has been omitted in this perspective view. Shown here, the embodiment of the supply and discharge device 4, a feed cylinder 40 and a removal cylinder 41, which are releasably operatively connected respectively to the filling passage 104 and the output passage 105.

For maintenance purposes, the supply and discharge device 4 can be completely separated from the reactor 1 and be connected in the operating state according to liquid and pressure-tight with the reactor 1. The supply and discharge device 4 is releasably secured by flange on the reactor 1. A device bearing 42 is designed such that the supply and discharge device 4 is mounted relative to the reactor 1 aligned. Since the reactor 1 explained here is preferably rotated around the outer container longitudinal axis La during the course of the carbonization process, the device bearing 42 is designed such that the supply and discharge device 4 can be rotated during rotation of the reactor 1 about the outer container longitudinal axis La with the feed and discharge device 4 connected , To facilitate rotation, the device bearing 42 is height adjustable. A force regulator can optimally adjust the height of the device bearing 42 for rotation to be achievable.

So that the process medium in the form of educts can be fed and discharged in the form of the carbonization products, drive means 43 are provided on the supply and discharge device 4. The process medium can thereby be transferred in a controlled manner with a control, not shown.

As shown in the horizontal section through the reactor 1 according to FIG. 4, within the outer container 10, the mentioned Karbonisierungsbehälter 11 is stored completely embedded, wherein the Karbonisierungsbehälterlängsachse Lp coincides with the outer container longitudinal axis La together. This Karbonisierungsbehälter 11 is connected to the filling channel 1141 and the output channel 1142 fixed to the base bottom 1001 of the outer container 10 and thus immovably stored in the outer container shell 100 relative to the outer container 10.

The Karbonisierungsbehälter 11 has a Karbonisierungsbehältermantel 111, which is completely surrounded or lapped in the operating state of a fluid 3. In the interior of the Karbonisierungsbehälters 11 is in the operating state, the process medium 5 in the different states. The carbonizing container 11 includes a central shell portion which is disposed between a lid part 1101 and a bottom part 1105. The central shell portion is configured cylindrically shaped and the cover part 1101 by means of cover flange 1102 and the bottom part 1105 releasably secured by means of bottom flange 1106 on the central shell portion. The entire Karbonisierungsbehälter 11 is pressurized in the operating state with the process medium 5 under pressure and is carried out corresponding liquid and pressure-tight.

Subsequently, an output channel 1142 is connected to the bottom part 1105, which leads out of the interior of the Karbonisierungsbehälters 11. After installing the carbonation container 11 in the outer container 10, the discharge channel 1142 is arranged so as to be guided by the discharge passage 105 of the base tray 1001.

As shown in Fig. 5a, a filling channel 1141 is connected to the bottom part 1105, which is correspondingly feasible through the filling passage 104 in the base bottom 1001 of the outer container 10. The dispensing channel 1142 and the filling channel 1141 can be fastened by the base base 1001 so as to be unsolvable by means of a cohesive welded connection or detachable by means of flange connections to the base plate 1001. By fastening flanges 115 integrally formed on the filling channel 1141 and the outlet channel 1142, the channels 1141, 1142 can be connected to the supply and discharge device 4, which has been omitted in FIGS. 5a and 5b for the sake of clarity.

In the operating state, the process medium 5 is filled through the filling channel 1141 in the interior of the Karbonisierungsbehälters 11 and discharged after a dwell or reaction time through the output channel 1142 from the Karbonisierungsbehälter 11. Accordingly, filling and dispensing channel 1141, 1142 are opened only temporarily controlled during operation in order to influence the exothermic reaction of the hydrothermal carbonization only briefly. Thus, the internal pressure and the temperature in the carbonation container 10 is only briefly disturbed.

While in the carbonation 11, the hydrothermal carbonization proceeds under elevated temperature and elevated pressure, surrounds the fluid 3, which is in particular a thermal oil, the Karbonisierungsbehälter 11 within the closed outer container shell 100th

The thermal oil 3 is used in the hydrothermal carbonization here, inter alia, as a heat transfer fluid. A supply nozzle 106 arranged on the outer container 10 is used for filling and pressurizing the outer container interior 103 with the fluid 3. At the supply nozzle 106, spidery-like tubes 109 are provided in the outer container interior 103 for the flow guidance of the thermal oil 3. By means of vent pipe 108, the air can be discharged from the outer container interior 103 during filling. Thus externally heated thermal oil 3 can be supplied from a thermal oil tank, whereby the Karbonisierungsbehälter 11 can be brought to a temperature necessary for carbonization. Due to the temperature increase of the thermal oil 3, the exothermic reaction is started and maintained, since this takes place only from a minimum temperature. By measuring the temperature and the possibility of exchanging the fluid 3, the temperature in the carbonation container 11 can be controlled.

The thermal oil in the outer container 10 and the Karbonisierungsbehälter 11 form a heat exchanger. The high-viscosity solids-laden educts 5 and products 5 in the interior of the carbonation container 11 release their heat partly through the Karbonisierungsbehältermantel 110 during the hydrothermal carbonization to the surrounding thermal oil 3 from. The thermal oil 3 flows around the Karbonisierungsbehälter 11 and can absorb and release heat. If the Karbonisierungsbehälter 11 are cooled, according to excess heat energy can be used externally by means of thermal oil 3.

In order to ensure the passage of the process medium 5 through the interior of the Karbonisierungsbehälters 11 is a stirring and conveying device comprising an agitator 13, the interior at least partially arranged transversely. In operation, by means of agitator 13, a continuous mixing of the process medium 5, the educts and Karbonisierungsprodukte controlled from the outside take place. The agitator 13 also serves as a conveying device of the process medium 5. The agitator 13 can be designed in different ways. Agitator drive means 132 are provided to operate the agitator 13 from the outside in operation. By a drive bushing 107 in the outer container 10 and a transverse drive device 119 which leads to the agitator 13 in the Karbonisierungsbehälter 11, the agitator 13 is driven driven. Since the Karbonisierungsbehälter 11 is formed of several parts, the agitator 13 can be easily inserted into the Karbonisierungsbehälter 11, rotatably mounted there by means of agitator bearing 133 and actuated controlled from outside the reactor 1. The agitator 13 is here equipped with a friction wheel, which is shown in Fig. 5beingekreist. At the agitator 13 leaves are arranged as baffles and / or to support the axial promotion.

The Karbonisierungsbehälter 11 and the agitator 13 therein are designed so that the process medium 5, which comprises biomass in the form of sewage sludge and green waste, during the Karbonisierungsprozesses can be conveyed. The biomass is comminuted externally before being fed into the reactor, but solids with a maximum piece size of 2.5 cm × 2.5 cm × 2.5 cm remain as part of the process medium 5. By this solid loading 13 special requirements are placed on the Karbonisierungsbehälter 11 and the agitator.

Characterized in that the outer container 10 and the Karbonisierungsbehälter 11 are each formed in several parts, a simple assembly of the reactor 1 and thus the entire system at the site is possible. Above all, maintenance work can be carried out without great effort, since no manhole must be provided in order to have access to the containers 10, 11.

All walls and components which come into direct contact with the process medium 5 are made of acid-resistant material. Here these parts are made of stainless steel.

As can be seen in Fig. 5a, a heat transfer channel 116 is the Karbonisierungsbehälter 11 centric and completely crossing, arranged, or recessed from the Karbonisierungsbehälter hollow volume. The fluid 3 or thermal oil 3 surrounding the carbonation container 11 flows around the outer walls of the central shell section, the bottom part 1105 and the cover part 1101 of the carbonation tank 11. The design of the heat transfer channel 116 additionally surrounds the walls of the heat transfer channel 116 in the center of the carbonation tank 11. The interior of the heat transfer channel 116 is completely separated from the process medium 5. Heat energy is transferred through the walls of the heat transfer channel 116 indirectly to the process medium 5 and in the reverse direction. Accordingly, the thermal oil circulating in the interior of the heat transfer passage 116 absorbs or gives off heat.

The heat transfer channel 116 has an inlet 1161, which faces the bottom part 1105 of the Karbonisierungsbehälters 11. The thermal oil 3 can flow around the bottom part 1105 in the region of the filling channel 1141 and the outlet channel 1142. Also, the thermal oil 3 may flow from the inlet 1161 to an outlet 1162 facing the lid member 1101 through the heat transfer passage 116. Here, the walls of the heat transfer channel 116 are flat, parallel to each other and approximately parallel to the outer walls of Karbonisierungsbehälter 11 and concentric with the Karbonisierungsbehälterlängsachse Lp arranged. Thus, a heat transfer channel 116 is provided with concentric walls crossing the center of the Karbonisierungsbehälters 11. On the way between inlet 1161 and outlet 1162, heat is transferred to the circulating thermal oil 3 from the walls of the heat transfer channel 116, which come in contact with reactive process medium 5 inside.

The diameter and / or the cross-sectional area of the heat transfer channel 116 are selected to be at least approximately constant over the entire length l of the heat transfer channel 116. However, it is also possible to have an embodiment with cross-sectional areas that have varying sizes in the course of the heat transfer channel, or other means in the area of the walls of the heat transfer channel 116, which enlarge the active surface area. These could be shaped ribs on the surface of the walls that optimize heat transfer.

The diameter of the heat transfer channel 116 is here chosen so large that it is about one fifth to one quarter of the diameter of the entire Karbonisierungsbehälters 11 and the Karbonisierungsbehältermantels 110. This ensures that a sufficient amount of process medium 5 is still transportable through the interior of the Karbonisierungsbehälters 11 and sufficient amount of thermal oil 3 can flow through the interior of the heat transfer channel 116 for sufficient heat transfer.

The heat transfer channel 116 may be configured completely crossing the Karbonisierungsbehälter 11, wherein the longitudinal axis of the heat transfer channel 116 may also be arranged slightly different from the direction of the Karbonisierungsbehälterlängsachse Lp. Since a Karbonisierungsbehälter 11 with a heat transfer channel 116 perpendicular to the direction of Karbonisierungsbehälterlängsachse Lp is easy to produce, such a design would be possible.

It must be possible in any case that the thermal oil 3 completely flow through the heat transfer channel 116 and thus can cross the Karbonisierungsbehälter 11 and circulate surrounding. Then, the additionally achieved heat transfer surface of the heat transfer channel 116 can be optimally utilized.

If a heat transfer channel 116 is arranged in a carbonation container 11, the agitator 13 must be adapted accordingly. Here, the agitator 13 is designed with a Rührwerkwand tubular as a hollow cylindrical body which is rotatable about a conveying longitudinal axis within the Karbonisierungsbehälters 11 can be arranged. The agitator wall forms a completely closed cylindrical surface. In contrast to agitators of the prior art, the agitator 13 is formed without a centric shaft and forms a stable hollow cylindrical body whose size is adapted to the interior of the Karbonisierungsbehälters 11, so that the agitator wall is at least approximately parallel to the Karbonisierungsbehältermantel 110.

An inner delivery chamber is formed, which runs concentrically to the longitudinal axis and in which the process medium 5 is moved parallel to the heat transfer channel 116 by inner leaves. Through this inner delivery chamber, the process medium is conveyed away from the inlet side of the Karbonisierungsbehälters 11. On its way, the process medium 5 can be optimally heated by a small distance to the heat transfer channel 116, whereby the Karbonisierungsreaktion is started.

In the region of the cover part 1101 of the Karbonisierungsbehälters 11, the process medium 5 is deflected in a deflection section and enters a concentric outer delivery chamber, which is formed between agitator wall and inner wall of the Karbonisierungsbehälters 11. Due to the arrangement of outer sheets on the outer surface of the agitator wall, the process medium 5 is conveyed concentrically in the direction of the discharge channel 1142 in the bottom flange 1106. The fact that process medium 5 is guided close to the inner wall of the Karbonisierungsbehälters 11, an improved heat transfer between highly heated process medium 5 and the wall of the Karbonisierungsbehälters 11 and the thermal oil 3, which surrounds this wall, take place.

LIST OF REFERENCE NUMBERS

[0047] <Tb> 1 <sep> reactor <tb> <sep> 10 <sep> External container (rigid, as pressure vessel, storage container, also spherical possible) <Tb> <sep> <sep> 100 <sep> outer container cladding <tb> <sep> <sep> <sep> 1001 <sep> Base Floor <tb> <sep> <sep> <sep> 1002 <sep> Base flange <tb> <sep> <sep> <sep> 1003 <sep> cylindrical center piece <tb> <sep> <sep> <sep> 1004 <sep> Lid base flange <tb> <sep> <sep> <sep> 1005 <sep> Lid base (curved, e.g., torispheric) <Tb> <sep> <sep> 103 <sep> Foreign container interior <Tb> <sep> <sep> 104 <sep> Einfülldurchführung <Tb> <sep> <sep> 105 <sep> Output implementation <tb> <sep> <sep> 106 <sep> Bypass Socket <Tb> <sep> <sep> 107 <sep> Drive Through <Tb> <sep> <sep> 108 <sep> vent connection <Tb> <sep> <sep> 109 <sep> Pipes <Tb> <sep> <sep> La <sep> outer container longitudinal axis <Tb> <sep> 11 <sep> KarbonisierungsbehäIter <tb> <sep> <sep> 110 <sep> KarbonisierungsbehäImantel (at least two parts, here three parts, bell-shaped) <tb> <sep> <sep> <sep> 1101 <sep> Cover part (curved) <tb> <sep> <sep> <sep> 1102 <sep> Cover flange central (cylindrical) shell section <tb> <sep> <sep> <sep> 1103 <sep> first shell part <tb> <sep> <sep> <sep> 1104 <sep> second shell part <Tb> <sep> <sep> <sep> 1105 <sep> base part <Tb> <sep> <sep> <sep> 1106 <sep> bottom flange <Tb> <sep> <sep> <sep> 1141 <sep> launder <Tb> <sep> <sep> <sep> 1142 <sep> Output channel <tb> <sep> <sep> 115 <sep> Mounting flange (carbonation tank on base floor) <tb> <sep> <sep> 116 <sep> Heat transfer channel (variable in length, fully traversing) <Tb> <sep> <sep> <sep> 1161 <sep> inlet <tb> <sep> <sep> <sep> 1162 <sep> Outlet <Tb> <sep> <sep> 119 <sep> Gear <Tb> <sep> <sep> 120 <sep> Karbonisierungsbehälterlager <Tb> <sep> <sep> Lp <sep> Karbonisierungsbehälterlängsachse <Tb> <sep> 13 <sep> agitator <Tb> <sep> <sep> 132 <sep> Rührwerkantriebsmittel <Tb> 2 <sep> reactor storage device <Tb> <sep> 20 <sep> frame <Tb> <sep> 21 <sep> pivot <Tb> <sep> 22 <sep> rotary drive <Tb> 3 <sep> Fluid <tb> 4 <sep> Supply and discharge device <Tb> <sep> 40 <sep> feed cylinder <Tb> <sep> 41 <sep> sampling cylinder <tb> <sep> 42 <sep> Device Bearing (rotatable) <Tb> <sep> 43 <sep> drive means <tb> 5 <sep> process medium (highly viscous and solids laden) <tb> <sep> Fillings / eduts / carbonation products / each with process water

Claims (7)

A carbonator vessel (11) comprising a carbonization vessel cavity volume enclosed by a carbonation vessel shell (110) for hydrothermal carbonation of a high viscosity and / or solids loaded process medium (5), wherein the carbonation vessel shell (110) is storable in a fluid (3), wherein process medium (5 ) and fluid (3) are separated from each other, characterized in that a heat transfer channel (116) is arranged to completely cross the carbonation container (11), from an inlet (1161) to an outlet (1162), the interior of the heat transfer channel (11) 116) completely by means of walls of the heat transfer channel (116) of filled process medium (5) separable and the fluid (3) can be flowed through. 2. Karbonisierungsbehälter (11) according to claim 1, wherein the heat transfer channel (116) is arranged at least approximately centrally through the Karbonisierungsbehälter (11) extending. A carbonator vessel (11) according to claim 2, wherein the walls of the heat transfer passage (116) are concentric with the carbonization vessel longitudinal axis (Lp). 4. carbonization container (11) according to any one of the preceding claims, wherein the diameter and / or the cross-sectional area of the heat transfer channel (116) remains at least approximately constant over its entire length (I). A carbonator vessel (11) according to any one of claims 1 to 3, wherein the cross-sectional area of the heat transfer passage (116) varies along the path of the heat transfer passage (116) or means are provided in the area of the walls of the heat transfer passage (116) enlarging the active area. A carbonator vessel (11) according to any one of the preceding claims, wherein the maximum diameter of the heat transfer passage (116) is about one fifth to one quarter the diameter of the carbonation vessel (11). 7. reactor (1) comprising a Karbonisierungsbehälter (11) with a completely crossing heat transfer channel (116) according to one of the preceding claims.