Reactor for supercritical hydrothermal gasification of biomass

Abstract

The invention relates to a reactor 1 for supercritical hydrothermal gasification of aqueous multi-component mixtures under oxygen-free conditions. The invention further relates to a system for operating the reactor 1, a method for operating the reactor 1, and the use of the reactor 1. The reactor 1 according to the invention is compatible with many existing systems, is compact in construction, can be set up to be easy to use, and can be economically manufactured and operated. Thus, the reactor 1 according to the invention enables for the first time a diversified commercial use of the hydrothermal gasification of biomass, sewage sludge and other organic waste in supercritical water.

Description

[0001] The present invention relates to a reactor for supercritical hydrothermal gasification of an aqueous multi-component mixture under oxygen-free conditions. It is a further object of the present invention to provide a system for operating the reactor, a method for operating the reactor, and the use of the reactor. The reactor according to the present invention is compatible with many existing systems, compact in construction, can be provided as a turnkey solution, and can be manufactured and operated at low cost. Thus, the reactor according to the present invention enables for the first time a plurality of commercial uses of the hydrothermal gasification of biomass, sludge and other organic waste in supercritical water.

[0002] By appropriate selection of the process parameters, it is possible to produce the energy carriers hydrogen and methane from biomass and organic waste by supercritical hydrothermal gasification in supercritical water at pressures > 25 MPa and temperatures of 600 to 700 °C without the addition of catalysts and in the absence of oxygen. The biomass or organic waste used as a reactant is usually a multi-component mixture of unknown composition. In addition to a variety of organic compounds, the biomass or organic waste also includes other valuable materials, such as metals, metal salts and inorganic compounds such as sand. It is advantageous to separate the valuable materials present in the aqueous multi-component mixture from the aqueous biomass prior to supercritical hydrothermal gasification. This is known from WO 2019 / 020209.

[0003] Reactors for supercritical hydrothermal gasification are disclosed in DE 20220307 U1, DE 29719196 U1, DE 29913370 U1, DE 10217165 A1, DE 102005037469 A1, DE 102006044116 B3, DE 102008028788 A1.

[0004] The process conditions and requirements for reactors for supercritical hydrothermal gasification of biomass are high due to the high pressure, the high temperature and the reactants used. Therefore, reactors for supercritical hydrothermal gasification have to be specially adapted and / or regularly updated or cleaned. The high temperature of supercritical hydrothermal gasification promotes the corrosion processes of the reactor. Therefore, the materials of the reactor have to be resistant to high temperatures, corrosion and pressure. Materials that are resistant to high temperatures and corrosion are known. However, these materials are not pressure-resistant in the relevant temperature range > 600 °C.

[0005] US 2009 / 127209 A1 discloses a reactor for the hydrothermal oxidation of aqueous waste material with the addition of an oxidizing agent, preferably air, at pressures above 22.1 MPa and temperatures above 374 °C. The reactor comprises a corrosion-resistant inner shell, an outer shell and pressure water between the shells, a stirring turbine attached to the bottom of the reactor, the central shaft and the plurality of blades of which extend over the entire length of the reactor to all parts of the inner shell. At the outlet of the reactor there is a filter device connected to a heat exchanger.

[0006] Another problem with supercritical hydrothermal gasification of biomass is that heating changes the solubility of the salts it contains, which can precipitate or precipitate in supercritical water, clogging the reactor.

[0007] CN 102503013 also discloses a reactor for hydrothermal oxidation of waste materials. The reactor has an inner corrosion-resistant shell and an outer pressure-resistant shell with water between the shells. Inside the inner shell, there is a heating wire and a hydrocyclone for separating solids, an outlet for brine, and a multiphase catalyst. The hydrocyclone is located upstream of the multiphase catalyst and is used to separate salts before oxidation.

[0008] The aforementioned reactors are unsuitable for supercritical hydrothermal gasification, which is carried out at temperatures of 600 to 700 degrees Celsius, because these temperatures cannot be reached in the aqueous biomass flowing through them. Another disadvantage of hydrothermal oxidation is the necessity of using catalysts in the reactor, which are prone to deactivation and therefore require frequent replacement. Furthermore, in known reactors, the separation of inorganic components is incomplete or only occurs after the hydrothermal conversion. Compared to supercritical hydrothermal gasification under anaerobic conditions (where the syngas produced from organic compounds consists primarily of hydrogen, methane, carbon dioxide, and water), the syngas produced by hydrothermal oxidation contains significant amounts of carbon monoxide (CO).

[0009] DE102018104595A1 discloses supercritical hydrothermal gasification in a reactor having an inner container and an outer container, wherein the inner container is temperature and corrosion resistant, and the outer container is pressure resistant. DE102018104595A1 discloses the use of a nickel-based alloy as the inner container and the presence of gas compressed to the gasification pressure between the containers, thus preventing the inner container from being affected by pressure differences. The reactor disclosed in DE102018104595A1 forgoes salt separation before hydrothermal gasification, causing the reactor to quickly become clogged and unusable.

[0010] WO2019 / 020209 and DE21201800266 disclose apparatuses for supercritical hydrothermal gasification of biomass under anaerobic conditions, wherein, prior to supercritical hydrothermal gasification, the compressed biomass is heated to up to 550 degrees Celsius to completely separate the inorganic components, thus preventing solids and salts from clogging the reactor during the subsequent supercritical hydrothermal gasification process. However, the apparatuses required by WO2019 / 020209 and DE21201800266 are not suitable for compact designs.

[0011] These multiple requirements for reactors that hydrothermally gasify biomass in supercritical water have so far prevented the technology from being commercially used for the recovery of recyclable materials from aqueous organic waste and for energy production.

[0012] The objective of this invention is to provide a reactor for supercritical hydrothermal gasification of biomass that does not have the aforementioned drawbacks, thereby enabling the widespread commercial application of supercritical hydrothermal gasification technology for biomass and organic waste.

[0013] The reactor 1 according to the present invention solves this problem.

[0014] The present invention provides a reactor 1 for supercritical hydrothermal gasification of an aqueous multicomponent mixture to 25-35 MPa under anaerobic conditions, comprising a pressure-sealed inner shell 2. Within the inner shell 2 is a separation zone 3 for heating the compressed aqueous multicomponent mixture to up to 550 degrees Celsius and separating recyclable materials from the compressed aqueous multicomponent mixture. Within the inner shell 2 is a heating zone 4 for heating the compressed aqueous multicomponent mixture to 600-700 degrees Celsius after the separation of recyclable materials; the heating zone 4 preferably includes one or more heating devices. Within the inner shell 2 is a residence zone 5 for supercritical hydrothermal gasification of the compressed aqueous multicomponent mixture after heating to 600-700 degrees Celsius.

[0015] The reactor 1 according to the invention is inexpensive, can be compactly constructed, and can be readily transported to the site of use for operation. This enables the reactor 1 according to the invention to be used in various waste treatment, water treatment, and energy supply plants.

[0016] The reactor 1 according to the invention is suitable for supercritical hydrothermal gasification of an aqueous multicomponent mixture compressed to 25 to 35 MPa under anaerobic conditions. When the reactor 1 is operated as intended, the aqueous multicomponent mixture compressed to 25 to 35 MPa is heated to a maximum of 700 degrees Celsius within the reactor 1. The inner shell 2 forms a two-dimensional, complete or extensive boundary between the separation zone 3, heating zone 4, and residence zone 5 arranged inside the reactor 1 and the area outside the inner shell 2. According to the invention, the inner shell 2 of the reactor 1 forms a pressure space (= first pressure space 15). The first pressure space 15 can be sealed by pressure sealing. Thus, a pressure of 25 to 35 MPa is maintained within the first pressure space 15 of the separation zone 3, heating zone 4, and residence zone 5, i.e., during the heating and compression of the aqueous multicomponent mixture, the separation of recyclable materials from the compressed aqueous multicomponent mixture, and the further heating and compression of the aqueous multicomponent mixture until supercritical hydrothermal gasification, during supercritical hydrothermal gasification, and after supercritical hydrothermal gasification. To maintain pressure within the inner shell 2, the inner shell 2 can be sealed using a pressure seal. The inner shell 2 encloses the first pressure space 15 within itself. The first pressure space 15 within the reactor 1 includes a separation zone 3, a heating zone 4, and a residence zone 5, which are interconnected.

[0017] A compressible seal means that when the inner shell 2 is compressibly sealed, a set pressure of 25 to 35 MPa is maintained within the inner shell 2. The inner shell 2 can completely seal the separation zone 3, the heating zone 4, and the residence zone 5. A compressible seal means that the inner shell 2 can include openings or can be opened. For example, a pressurizable sealable inner shell 2 can include one or more connections to the outside, such as openings, like the opening of pipe 14, wherein the openings and the openings of pipe 14 are interconnected in a pressurizable sealable manner. In the reactor 1 according to the invention, all connections to the outside are connected to the inner shell 2 in such a way that the connection can be closed in a pressure-sealed manner. The openings of the inner shell 2 and / or the openings of pipe 14 can be closed in a pressure-sealed manner, for example, through valves. In a particular embodiment, the compressible sealable inner shell 2 is a single pressurized sealable inner shell 2.

[0018] In a particularly preferred embodiment, the reactor 1 according to the invention includes an outer shell 6 surrounding an inner shell 2. In a preferred embodiment where the reactor 1 includes an inner shell 2 and an outer shell 6, the outer shell 6 forms a second pressure space 16 because the outer shell 6 forms a planar and complete or extensive boundary between the inner shell 2 and the outside. In a particularly preferred embodiment of the reactor 1, the outer shell 6 is a shell 6 that can be sealed in a pressure-sealed manner. The outer shell 6 can completely surround the inner shell 2. Preferably, the outer shell 6 includes one or more connections to the outside, such as openings or openings to pipes 14. In a preferred embodiment of the reactor 1, all connections to the outside are connected to the outer shell 6, thereby allowing the connections to be made in a pressure-sealed manner.

[0019] The present invention provides a reactor 1 for supercritical hydrothermal vaporization of an aqueous multicomponent mixture compressed to 25 to 35 MPa under anaerobic conditions, comprising a pressure-sealed inner shell 2. Within the inner shell 2 is a separation zone 3 for heating the compressed aqueous multicomponent mixture to up to 550 degrees Celsius and separating recyclable materials from the compressed aqueous multicomponent mixture. Within the inner shell 2 is a heating zone 4 for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after separation of recyclable materials; the heating zone 4 preferably includes one or more heating devices. Within the inner shell 2 is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. An outer shell 6 surrounds the inner shell 2, and a second pressure space 16 exists between the inner shell 2 and the outer shell 6.

[0020] In other embodiments, the reactor 1 according to the invention includes an inner shell 2 but no outer shell 6. When the reactor 1 does not include the outer shell 6, the inner shell 2 adapts to the pressure difference between the inside and outside of the reactor 1.

[0021] In a particularly preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, there is a separation zone 3 with one or more means for heating the compressed aqueous multicomponent mixture to up to 550 degrees Celsius, and one or more means for separating recyclable materials from the compressed aqueous multicomponent mixture. In the heating zone within the inner shell 2, there is preferably one or more means for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the separation of recyclable materials. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 2, heating zone 4, and residence zone 5 are arranged in a columnar configuration. The reactor 1 may include a compressibly sealable outer shell 6 surrounding the inner shell 2 and a second pressure space 16 between the inner shell 2 and the outer shell 6.

[0022] Internal components, such as heating and separation devices, are arranged in the form of hollow, elongated columns, referred to as columns. In a particularly preferred embodiment of the reactor 1 according to the invention, the separation zone 3, heating zone 4, and residence zone 5 are arranged in a columnar shape within the inner shell 2. This column is a process engineering device used for separation based on the physical properties and equilibrium states between different phases. In a particularly preferred embodiment of the reactor 1 according to the invention, the inner shell 2 includes column walls. In other particularly preferred embodiments of the reactor 1 according to the invention, the inner shell 2 is a column wall. Within the column, an aqueous multicomponent mixture compressed to 25 to 35 MPa first flows through the separation zone 3, then through the heating zone 4, and then through the residence zone 5 of the reactor 1 according to the invention. Within the column, the heating zone 4 is adjacent to the separation zone 3, and the residence zone 5 is adjacent to the heating zone 5.

[0023] The apparatus for heating the compressed aqueous multicomponent mixture is preferably a heating element, such as a heat exchanger or an electric heater, and the apparatus for separating recyclable materials is preferably a collector or separator. To separate recyclable materials from the compressed aqueous multicomponent mixture in separation zone 3, the column includes internal devices such as heat exchangers and collectors and / or separators. In separation zone 3, the column may include additional heating elements for further heating the compressed aqueous multicomponent mixture. In separation zone 3, heating zone 4, and residence zone 5, the column may include further internal devices. A particularly preferred embodiment of the reactor 1 according to the invention is that the various internal devices are arranged in a column. In a particularly preferred embodiment, the column (reactor 1) is upright. Arranging the reactor 1 as an upright column is particularly advantageous because, for example, in the separation zone, volatile components contained in the aqueous multicomponent mixture rise in the upright column, while recyclable materials (e.g., solids, metal salts, phosphates, and ammonium compounds) descend in the column and can be easily separated.

[0024] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, there is a separation zone 3 containing one or more heat exchangers for heating the compressed aqueous multicomponent mixture to up to 550 degrees Celsius, and one or more collectors or separators for separating recyclable materials from the compressed aqueous multicomponent mixture. Within the inner shell 2, there is a heating zone 4 with one or more heating elements for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the separation of recyclable materials. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal gasification of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are arranged in a columnar configuration. The reactor 1 may include an outer shell 6 surrounding the inner shell 2 and a second pressure space 16 located between the inner shell 2 and the outer shell 6. In a particularly preferred embodiment, the column is upright.

[0025] The reactor 1 according to the present invention may include different combinations of internal structures and detailed designs of molds. Various detailed embodiments can be adapted to different process requirements, different aqueous multi-component mixtures, and different applications. Examples of different embodiments of the reactor 1 according to the present invention are given below. However, the present invention is not limited to the disclosed embodiments.

[0026] In a particularly preferred embodiment of the reactor 1 according to the invention, one or more heating elements and one or more separators in the separation zone 3, and one or more heating elements in the heating zone 4 are arranged in a columnar internal configuration. In the reactor 1, the separator zone 3 is connected to the heating zone 4, and the heating zone 4 is connected to the residence zone 5. Through this arrangement in the reactor 1, the compressed aqueous multicomponent mixture first flows through the heating elements and separators in the separator zone 3, thereby separating recyclable material, and then flows through the heating zone 4, whereby the compressed aqueous multicomponent mixture is heated to a vaporization temperature of 600 to 700 degrees Celsius. The heated zone 4 then enters the residence zone 5, through which the aqueous multicomponent mixture flows and is thereby converted into syngas and water. Supercritical hydrothermal vaporization of the aqueous multicomponent mixture compressed to 25 to 35 MPa takes place in the reactor 1 at a temperature of 600 to 700 degrees Celsius (equivalent to the vaporization temperature), i.e., during the transition from the heating zone 4 to the residence zone 5 and within the residence zone 5 itself.

[0027] Reactor 1 includes heating elements and separators for separating recyclable materials from a compressed aqueous multicomponent mixture. These elements are arranged in reactor 1 to separate the recyclable materials from the compressed aqueous multicomponent mixture before supercritical hydrothermal gasification. During this process, when the temperature rises to 550 degrees Celsius, the recyclable materials separate from the compressed aqueous multicomponent mixture and precipitate. By separating recyclable materials such as sand, salt, and nutrients from the compressed aqueous multicomponent mixture before heating to above 550 degrees Celsius, or separating recyclable materials such as sand, salt, and nutrients in separation zone 3 of reactor 1 before heating to a gasification temperature of 600 to 700 degrees Celsius, substances contained in the aqueous multicomponent mixture that could potentially clog reactor 1 in heating zone 4 and / or residence zone 5 and significantly contribute to corrosion at high temperatures are essentially separated. After the recyclable materials are separated, the aqueous multicomponent mixture consists primarily of organic compounds and components. This prevents clogging of reactor 1 and reduces corrosion of reactor 1.

[0028] A compact design of reactor 1 is also possible by arranging the separation zone 3, heating zone 4, and residence zone 5 of reactor 1 according to the invention in a columnar shape. The height or length of reactor 1 according to the invention is, for example, 30 meters, 25 meters, preferably 20 meters or 17 meters, or less, for example, 10 meters or 5 meters. For example, the diameter of reactor 1 is 3 meters or less, for example, 0.5 to 2.5 meters, preferably 1 to 2 meters, for example, 1.5 meters, 1.6 meters, 1.7 meters, 1.8 meters, or 1.9 meters. In a preferred embodiment, the diameter of reactor 1 is 1.2 meters to 2.5 meters, preferably 1.8 meters.

[0029] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by compression. Within the inner shell 2, there is a separation zone 3 containing one or more heat exchangers for heating the compressed aqueous multicomponent mixture to up to 550 degrees Celsius, and one or more collectors or separators for separating recyclable materials from the compressed aqueous multicomponent mixture. The inner shell 2 also contains a heating zone 4 for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the separation of recyclable materials; the heating zone 4 preferably includes one or more heating elements. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal gasification of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are arranged in a columnar configuration. The reactor 1 has a height of 30 meters or less and a diameter of 2.5 meters or less. In a specific embodiment, the reactor 1 has a height of 15 to 20 meters and a diameter of 1 to 2 meters. In a particular embodiment, reactor 1 has a length of 17 meters and a diameter of 1.8 meters. Reactor 1 may include an outer shell 6 surrounding the inner shell 2 and a second pressure space 16 between the inner shell 2 and the outer shell 6.

[0030] In a preferred embodiment of reactor 1, the valuable material component WF1 is separated from the multicomponent mixture compressed to 25 to 35 MPa in separation zone 3 at 400 to 550 degrees Celsius. In another embodiment of reactor 1, the valuable material component WF1 is separated from the aqueous multicomponent mixture compressed to 25 to 35 MPa in separation zone 3 at 300 to 550 degrees Celsius. In yet another embodiment of reactor 1, the valuable material component WF1 is separated from the aqueous multicomponent mixture compressed to 25 to 35 MPa in separation zone 3 at 300 to 400 degrees Celsius. In yet another embodiment of reactor 1, the valuable material component WF1 is separated from the aqueous multicomponent mixture compressed to 25 to 35 MPa in separation zone 3 at a temperature of 200 to 400 degrees Celsius. To this end, the reactor 1 according to the invention includes a separation zone 3 within an inner shell 2. The separation zone 3 includes a heat exchanger WT1 9 for heating the compressed aqueous multicomponent mixture to a temperature selected from 400 to 550 degrees Celsius, 300 to 550 degrees Celsius, 300 to 400 degrees Celsius, and 200 to 400 degrees Celsius, and a separator A1 for separating valuable material components WF1 from the compressed aqueous multicomponent mixture. When the aqueous multicomponent mixture compressed to 25 to 35 MPa is heated to at least 200 degrees Celsius, for example 300, preferably 400 to 550 degrees Celsius, at least one valuable material component WF1, such as recyclable materials, solids, metal salts, or nutrients, is separated from the compressed aqueous multicomponent mixture.

[0031] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT1 9 for heating the compressed aqueous multicomponent mixture to 200 to 550 degrees Celsius, preferably 400 to 550 degrees Celsius, and a separator A1 for separating the valuable material component WF1 from the compressed aqueous multicomponent mixture. The inner shell 2 also includes a heating zone 4 for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the separation of the valuable material component WF1; the heating zone 4 preferably includes one or more heating elements. Within the inner shell 2, a residence zone 5 is provided for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are preferably arranged in a columnar configuration. The reactor 1 may include an outer shell 6 surrounding the inner shell 2 and a second pressure space 16 between the inner shell 2 and the outer shell 6.

[0032] In another preferred embodiment of reactor 1 according to the invention, the recyclable material is separated into one or more valuable material components, such as two, three, or more valuable material components. Whether one or more valuable material components are separated depends, for example, on the aqueous multicomponent mixture used, i.e., the composition of the aqueous multicomponent mixture and / or the further use of the separated recyclable material. Reactor 1 according to the invention can be adapted accordingly by those skilled in the art. In a preferred embodiment of reactor 1 according to the invention, for this purpose, the temperature of separation zone 3 is heated in one or more steps by one or more heating elements, such as heat exchangers, through which the compressed aqueous multicomponent mixture flows, and the recyclable material is separated into one or more fractions. For this purpose, reactor 1 according to the invention includes one or more heating elements, such as heat exchangers, and a separator and / or collector for valuable material components.

[0033] In a particularly preferred embodiment, reactor 1 includes multiple heating elements, such as heat exchangers, and multiple collectors and / or separators in separation zone 3 for separating multiple valuable material components from a multicomponent mixture compressed to 25 to 35 MPa.

[0034] In a particularly preferred embodiment, reactor 1 includes two heating devices and two devices for separating two valuable material components from an aqueous multicomponent mixture compressed to 25 to 35 MPa in separation zone 3. In one embodiment, reactor 1 according to the invention includes separation zone 3 in inner shell 2, which includes heat exchanger WT19 for heating the compressed aqueous multicomponent mixture to a temperature up to 550 degrees Celsius, preferably 400 to 550 degrees Celsius, and separator A1 for separating valuable material component WF1 from the compressed aqueous multicomponent mixture. In separation zone 3, heat exchanger WT212 is used to heat the compressed aqueous multicomponent mixture to a temperature up to 400 degrees Celsius, preferably 200 to 400 degrees Celsius or 300 to 400 degrees Celsius, and separator A2 is used to separate valuable material component WF2 from the compressed aqueous multicomponent mixture. The heat exchangers WT1 9 and WT2 12 are arranged such that the compressed aqueous multicomponent mixture first flows through heat exchanger WT2 12 and is heated to 400 degrees Celsius, then flows through heat exchanger WT1 9 and is heated to 550 degrees Celsius. In a particularly preferred embodiment of reactor 1, heat exchangers WT1 9 and WT2 12 are arranged in the column such that the compressed aqueous multicomponent mixture first flows through heat exchanger WT2 12 and is heated to 400 degrees Celsius, where the valuable component WF2 is separated, then flows through heat exchanger WT1 9 and is heated to 550 degrees Celsius, where the valuable component WT1 is separated. Other alternative heating and separation processes are known to those skilled in the art.

[0035] In a particularly preferred embodiment, reactor 1 includes three heating devices and three devices in separation zone 3 for separating three valuable material components from an aqueous multicomponent mixture compressed to 25 to 35 MPa. In a particularly preferred embodiment, the reactor 1 according to the invention includes a separation zone 3 in an inner shell 2, the separation zone 3 including a heat exchanger WT1 9 for heating the compressed aqueous multicomponent mixture to a maximum of 550 degrees Celsius, preferably 400 to 550 degrees Celsius; and a separator A1 for separating the valuable material component WF1 from the compressed aqueous multicomponent mixture; in the separation zone 3, a heat exchanger WT2 12 is used to heat the compressed aqueous multicomponent mixture to a maximum of 400 degrees Celsius, preferably 300 to 400 degrees Celsius, and a separator A2 is used to separate the valuable material component WF2 from the compressed aqueous multicomponent mixture; in the separation zone 3, a heat exchanger WT3 13 is used to heat the compressed aqueous multicomponent mixture to a temperature up to 300 degrees Celsius, preferably 200 to 300 degrees Celsius, and a separator A3 separates the valuable material component WF3 from the compressed aqueous multicomponent mixture. In reactor 1, heat exchangers WT1 9, WT2 12, and WT3 13 are interconnected, preferably arranged in a columnar configuration. The compressed aqueous multicomponent mixture first flows through heat exchanger WT3 13, where it is heated to 300 degrees Celsius, separating the valuable material component WF3. It then passes through heat exchanger WT2 12, where it is heated to 400 degrees Celsius, separating the valuable material component WF2. Finally, it passes through heat exchanger WT1 9, where it is heated to 550 degrees Celsius, separating the valuable material component WF1. According to the invention, those skilled in the art can realize other possibilities for the stepwise heating of the compressed aqueous multicomponent mixture and the separation of valuable material components in a correspondingly adapted reactor 1.

[0036] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT2 12 for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius, preferably 300 to 400 degrees Celsius; and a separator A2 for separating the valuable material component WF2. Heat exchangers WT2 12 and WT1 9 are interconnected, allowing the compressed aqueous multicomponent mixture to first flow through heat exchanger WT2 12 and then through heat exchanger WT1 9. Within the inner shell 2, a heating zone 4 is provided for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after separating the valuable material components WF2 and WF1. This heating zone preferably includes one or more heating elements. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of a compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are arranged in a columnar configuration. The reactor 1 may include an outer shell 6 surrounding the inner shell 2 and a second pressure space 16 between the inner shell 2 and the outer shell 6.

[0037] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT3 13 and a separator A3 for heating the compressed aqueous multi-component mixture to 300 degrees Celsius, preferably 200 to 300 degrees Celsius, and for separating the valuable material component WF3; and a heat exchanger WT2 12 and a separator A2 for heating the compressed aqueous multi-component mixture to 400 degrees Celsius, preferably 300 to 400 degrees Celsius, and for separating the valuable material component WF2. Heat exchangers WT1 9 and separator A1 are used to heat the compressed aqueous multicomponent mixture to a maximum of 550 degrees Celsius, preferably 400 to 550 degrees Celsius, and to separate the valuable material component WF1. Heat exchangers WT3 13, WT2 12, and WT1 9 are interconnected, such that the compressed aqueous multicomponent mixture first flows through heat exchanger WT3 13, then through heat exchanger WT2 12, and finally through heat exchanger WT19. In the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the separation of valuable material components WF3, WF2, and WF1. Heating zone 4 preferably includes one or more heating elements. In the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are arranged in a columnar shape. The reactor 1 may include an outer shell 6 surrounding the inner shell 2 and a second pressure space 16 between the inner shell 2 and the outer shell 6.

[0038] According to the reactor 1 of the present invention, inorganic and solid recyclable materials can be separated from an aqueous multicomponent mixture consisting of organic and inorganic components, and the recyclable materials can be used for new purposes. A corresponding process for separating three parts of recyclable materials from an aqueous multicomponent mixture is known from EP 3434382 B1.

[0039] The reactor 1 according to the invention is characterized in that, prior to supercritical hydrothermal gasification, recyclable materials (valuable materials) are separated from the aqueous multi-component mixture. Therefore, on the one hand, the recyclable materials are recovered and can be sent for further utilization (recycling). Simultaneously, this minimizes the clogging of reactor 1 by precipitated salts and solids, extending the service life of reactor 1 and other components. Corrosion of reactor 1 is also significantly reduced.

[0040] Recyclable materials in the sense of this invention are, for example, all inorganic components contained in their respective multi-component mixtures, such as phosphorus, for example in the form of phosphate, nitrogen, for example in the form of ammonium, metals, for example in the form of metal ion salts, heavy metals, for example in the form of heavy metal ion salts, silicon, for example in the form of sand, and calcium, for example in the form of sand.

[0041] Reactor 1 can be used to separate recyclable materials from one or more fractions from a compressed aqueous multicomponent mixture. Among three valuable material components WF3, WF2, and WF1, solid matter is enriched in valuable material component WF3, metal salts in valuable material component WF2, and phosphates and ammonium in valuable material component WF1. This is provided that the multicomponent mixture as reactants includes the aforementioned recyclable materials.

[0042] When recyclable materials from two valuable material components, WF2 and WF1, are separated from a compressed aqueous multicomponent mixture, solids and metal salts are enriched in the valuable material component WF2, while phosphates and ammonium are enriched in the valuable material component WF1. This is provided that the multicomponent mixture serving as reactants includes the aforementioned recyclable materials.

[0043] When valuable material component WF1 is separated from a compressed aqueous multicomponent mixture, WF1 is rich in solids, metal salts, phosphates, and ammonium. The condition is that the multicomponent mixture used as reactants includes the aforementioned recyclable materials.

[0044] After the recyclable materials are separated, the aqueous multicomponent mixture consists mainly of or only of organic compounds or organic components and water. Following the separation of recyclable materials, the compressed aqueous multicomponent mixture is heated to a vaporization temperature of 600 to 700 degrees Celsius in heating zone 4. After separation, the compressed aqueous multicomponent mixture first flows through heating zone 4, then through residence zone 5, where it is vaporized into syngas. The syngas dissolves in supercritical water under the pressure and temperature conditions present in residence zone 5 during normal operation of reactor 1.

[0045] The reactor 1 according to the invention has a heating zone 4 in the inner shell 2 through which a compressed aqueous multicomponent mixture flows after the valuable material components have been separated. In the heating zone 4, the compressed aqueous multicomponent mixture is heated to at least 600 degrees Celsius, for example 610 or 620 degrees Celsius, preferably 630 or 640 degrees Celsius, and particularly preferably 650 or 660 degrees Celsius. In the heating zone 4, the compressed aqueous multicomponent mixture is heated to a maximum of 700 degrees Celsius, for example 695 or 690 degrees Celsius, preferably 685 or 680 degrees Celsius, and particularly preferably 675 or 670 degrees Celsius. Those skilled in the art can vary the temperature according to the composition of the aqueous multicomponent mixture used and / or the desired composition of the syngas produced during supercritical hydrothermal gasification, for example. In a preferred embodiment, the reactor 1 according to the invention includes one or more heating elements in the heating zone 4 for this purpose. Heating of heating zone 4 can be provided by heating elements arranged inside the inner shell 2 of heating zone 4 and / or heating elements arranged outside the inner shell 2 near heating zone 4.

[0046] In a preferred embodiment, the reactor 1 according to the invention includes a heat exchanger WT4 10 as a heating element in the inner shell 2 of the heating zone 4. The reactor 1 according to the invention may include further heat exchangers in the heating zone 4.

[0047] In a preferred embodiment, heating of the compressed aqueous multicomponent mixture in separation zone 3 and at least partially in heating zone 4 is carried out using a heat exchanger, whereby the heat from the supercritical water containing the syngas is used to heat the compressed aqueous multicomponent mixture. For this purpose, in the reactor 1 according to the invention, the supercritical water containing the syngas is drawn from residence zone 5 and passed through the heat exchanger. In a preferred embodiment of reactor 1, this is done either by a single syngas conduit 11 arranged within reactor 1 and connected to the heat exchanger, or by several syngas conduits 11 arranged within reactor 1 and connected to the heat exchanger. Thus, the compressed aqueous multicomponent mixture (= reactants) is heated while the supercritical water containing the syngas is cooled. The conduction of the supercritical water containing the syngas within reactor 1, and the utilization of the heat contained in the supercritical water to heat new reactants, make reactor 1 according to the invention particularly energy efficient. The syngas conduit 11 and the heat exchanger prevent the compressed aqueous multicomponent mixture (= reactants) from mixing with the supercritical water containing the syngas (= products).

[0048] In a preferred embodiment, reactor 1 includes means for regulating the heat transferred by the heating element (preferably a heat exchanger, such as heat exchanger WT4 10) to the compressed aqueous multicomponent mixture in heating zone 4. In a preferred embodiment, reactor 1 includes means for regulating the heat transferred by the heating element (preferably a heat exchanger) to the compressed aqueous multicomponent mixture in separation zone 3. In a preferred embodiment, reactor 1 includes means for regulating the amount of supercritical water dissolved in syngas, which passes through the respective heat exchangers in heating zone 4 and / or separation zone 3.

[0049] A preferred means for regulating the amount of supercritical water containing syngas is a bypass valve that allows the supercritical water to flow through or bypass heat exchanger WT4 10. In a particularly preferred embodiment, the reactor 1 according to the invention includes a heat exchanger WT4 10 located in the inner shell 2 of the heating zone 4 and a bypass valve for regulating the amount of supercritical water flowing from the residence zone 5 through the heating zone 4 to the separation zone 3. In a particularly preferred embodiment, the reactor 1 according to the invention includes a heat exchanger WT4 10 and a bypass in the inner shell 2 of the heating zone 4, bypassing the heat exchanger WT4 10, and a bypass valve for regulating the amount of supercritical water. The bypass valve is used to regulate the amount of supercritical water that flows through or bypasses heat exchanger WT4 10 directly into heat exchanger WT1 9 (i.e., bypassing heat exchanger WT4 10). The bypass valve is preferably a component of heat exchanger WT4 10. In a particularly preferred embodiment, the reactor 1 according to the invention includes a heat exchanger WT4 10 in the inner shell 2 of the heating zone 4, wherein the heat exchanger WT4 10 includes a bypass valve for regulating the temperature of the heat exchanger WT1 9. The bypass valve can be used to regulate the amount of supercritical water that bypasses the heat exchanger WT4 10 and enters the heat exchanger WT1 9 directly. In this way, the temperature in the heat exchanger WT1 9 can be regulated. It is particularly critical that the compressed aqueous multicomponent mixture is heated to 550 degrees Celsius in the heat exchanger WT1 9. When little or no heat is transferred from the supercritical water dissolving syngas to the compressed aqueous multicomponent mixture in the heat exchanger WT4 10, the bypass and the bypass valve can be appropriately adjusted to increase the transferable heat flux of the compressed aqueous multicomponent mixture transferred to the heat exchanger WT1 9. Because the temperature difference between the supercritical water containing dissolved synthesis gas around the heat exchanger and the compressed aqueous multicomponent mixture inside the heat exchanger WT1 9 is large, if the supercritical water containing dissolved synthesis gas flows into the heat exchanger WT1 9 in the separation zone 3 through the bypass from the heating zone 4 more often than the supercritical water first flows through the heat exchanger WT4 10 and then through the heat exchanger WT1 9, the transferable heat flow inside the heat exchanger WT1 9 will increase.

[0050] For example, a WT4 10 heat exchanger with a bypass valve allows supercritical water containing dissolved syngas to pass completely through the WT4 10 heat exchanger and then through the WT1 9 heat exchanger for heating a compressed aqueous multicomponent mixture. In another bypass valve configuration, only partially dissolved syngas supercritical water passes through heat exchanger WT4 10, while the remaining partially dissolved syngas supercritical water enters the bypass and from there enters heat exchanger WT1 9. The bypass can be arranged, for example, between heat exchanger WT4 10 and the inner shell 2 of reactor 1. In yet another bypass valve configuration, the supercritical water containing dissolved syngas is completely introduced into the bypass and passes through heat exchanger WT1 9. These configurations are exemplary. Other bypass valve configurations are also possible.

[0051] In a preferred embodiment of the reactor 1 according to the invention, a bypass and a heat exchanger WT410 with a bypass valve are arranged near the separation zone 3 in the inner shell 2. The bypass and heat exchanger WT410 are connected to the separation zone 3. In a preferred embodiment of the reactor 1, the heat exchanger WT410 with a bypass valve is located near the separation zone 3, through which a compressed aqueous multicomponent mixture heated to 550 degrees Celsius flows after the valuable material component WT1 has been separated, thereby being further heated in the heat exchanger WT410 from 550 degrees Celsius, for example to 560 degrees Celsius, 570 degrees Celsius, 580 degrees Celsius, 590 degrees Celsius, 600 degrees Celsius, 610 degrees Celsius, 620 degrees Celsius or higher. The reactor 1 according to the invention may include further heating elements, such as one or more electric heaters, in the inner shell 2 of the heating zone 4.

[0052] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, there is a separation zone 3 containing one or more heat exchangers for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius, and one or more separators for separating recyclable materials from the compressed aqueous multicomponent mixture. Within the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the separation of recyclable materials; and includes a heat exchanger WT4 10, a bypass, and a bypass valve for temperature regulation of the separation zone 4. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are arranged in a columnar configuration. The reactor 1 may include an outer shell 6 surrounding the inner shell 2 and a second pressure space 16 between the inner shell 2 and the outer shell 6.

[0053] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT3 13 and a separator A3 for heating a compressed aqueous multicomponent mixture to a temperature up to 300 degrees Celsius and separating the valuable material component WF3; a heat exchanger WT2 12 and a separator A2 for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius and separating the valuable material component WF2; and a heat exchanger WT1 9 and a separator A1 for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius and separating the valuable material component WF1. Within the inner shell 2, a heating zone 4 is provided for heating the compressed aqueous multicomponent mixture after separation of the valuable material components WF3, WF2, and WF1 to 600 to 700 degrees Celsius and for regulating the temperature in the heat exchanger WT1 9. This heating zone 4 includes a bypass, a heat exchanger WT4 10, and a bypass valve. The inner shell 2 contains a residence zone 5 for supercritical hydrothermal vaporization of a compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are arranged in a columnar configuration. The reactor 1 may include an outer shell 6 surrounding the inner shell 2 and a second pressure space 16 between the inner shell 2 and the outer shell 6.

[0054] In a preferred embodiment of the reactor 1 according to the invention, the compressed aqueous multicomponent mixture is heated in the heating zone 4 by one or more heating elements arranged outside the inner shell 2 of the reactor 1. In a particularly preferred embodiment, the reactor 1 according to the invention includes an outer shell 6 surrounding the inner shell 2, a second pressure space 16 between the inner shell 2 and the outer shell 6, and one or more heating elements in the second pressure space 16 for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius in the heating zone 4. In a preferred embodiment of the reactor 1, the compressed aqueous multicomponent mixture in the heating zone 4 is heated in the heating zone 4 by one or more heating elements arranged in the second pressure space 16 between the inner shell 2 and the outer shell 6 of the reactor 1. In a preferred embodiment of the reactor 1, the compressed aqueous multicomponent mixture in the heating zone 4 is heated in the heating zone 4 by one or more electric heaters arranged in the second pressure space 16 between the inner shell 2 and the outer shell 6 of the reactor 1, which heat the aqueous multicomponent mixture in the heating zone 4 from outside the inner shell 2.

[0055] In one embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes one or more heat exchangers for heating a compressed aqueous multicomponent mixture to up to 550 degrees Celsius, and one or more separators for separating recyclable materials from the compressed aqueous multicomponent mixture. Within the inner shell 2, a heating zone 4 is provided for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the separation of recyclable materials. Within the inner shell 2, a residence zone 5 is provided for supercritical hydrothermal gasification of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are arranged in a row. An outer shell 6 surrounds the inner shell 2, and a second pressure space 16 exists between the inner shell 2 and the outer shell 3. Outside the inner shell 2, one or more heating elements are arranged in the second pressure space 16 for heating the compressed aqueous multicomponent mixture in zone 4.

[0056] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT3 13 and a separator A3 for heating the compressed aqueous multicomponent mixture to 300 degrees Celsius and separating the valuable material component WF3; a heat exchanger WT2 12 and a separator A2 for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius and separating the valuable material component WF2; and a heat exchanger WT1 9 and a separator A1 for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius and separating the valuable material component WF1. Within the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multicomponent mixture after separating the valuable material components WF3, WF2, and WF1 to 600 to 700 degrees Celsius. The heating zone 4 includes a heat exchanger WT4 10, a bypass, and a bypass valve for regulating the temperature in the heat exchanger WT1 9. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multi-component mixture after heating to 600-700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in a columnar shape, with the separation zone 3 located at the lower end of the column and the residence zone 5 at the upper end. An outer shell 6 surrounds the inner shell 2. A second pressure space 16 exists between the inner shell 2 and the outer shell 6. One or more heating elements are arranged in the second pressure space 16 surrounding the heating zone 4 to heat the compressed aqueous multi-component mixture in the heating zone 4 to 600-700 degrees Celsius.

[0057] In a preferred embodiment, reactor 1 includes a superheater in heating zone 4. In a preferred embodiment, reactor 1 includes an externally heated tubular section in heating zone 4, preferably electrically heated. In a preferred embodiment, reactor 1 in heating zone 4 includes a heat exchanger WT5, preferably a tubular heat exchanger. In a preferred embodiment, only a portion of heating zone 4 includes a superheater and / or an externally heated tubular section and / or a tubular heat exchanger. In a preferred embodiment of reactor 1, at least a portion of heating zone 4 includes an annular gap, designed as, for example, a superheater, a tubular section, or a tubular heat exchanger. In this portion of heating zone 4, the annular gap, such as a superheater, a tube segment, or a tubular heat exchanger, is arranged therein, through which the compressed aqueous multicomponent mixture is heated from both the outside and the inside. The compressed aqueous multicomponent mixture flowing through the annular gap in heating zone 4 is heated from the outside, preferably electrically, for example by one or more heating elements arranged in the second pressure space 16 between the inner shell 2 and the outer shell 6 of reactor 1, and from the inside by supercritical water containing dissolved syngas. Different phases are separated from each other through the annular gap.

[0058] In a preferred embodiment, supercritical water dissolved in syngas flows through a syngas conduit 11, which is arranged within the inner shell 2 of the heating zone 4. In a preferred embodiment of the reactor 1, the syngas conduit 11 passes through the heating zone 4, and at least in a portion of the heating zone 4, its diameter is almost equal to the diameter of the inner shell 2 within that region. Therefore, an annular gap remains between the syngas conduit 11 and the inner shell 2. The compressed aqueous multicomponent mixture flows through the annular gap between the syngas conduit 11 and the inner shell 2 in the heating zone 4, thereby being heated from the inside by the supercritical water dissolved in syngas through the syngas conduit 11. The compressed aqueous multicomponent mixture flows through the annular gap between the syngas conduit 11 and the inner shell 2 in the heating zone 4, thereby being heated from the outside by heating elements arranged in the second pressure space 16. This arrangement in the heating zone 4 has the advantage of providing a large surface area for heat transfer. Therefore, the compressed aqueous multicomponent mixture can be heated to the temperature of supercritical hydrothermal vaporization.

[0059] Preferably, the region in the second pressure space 16 where one or more heating elements are arranged surrounds the annular gap of the heating zone 4 for heating the compressed aqueous multicomponent mixture in the annular gap, while the compressed aqueous multicomponent mixture flows through the annular gap of the heating zone 4. The diameter of the annular gap refers to the distance from the outer wall of the synthesis gas pipe 11 to the inner wall of the inner shell 2. The annular gap can have different diameters at different locations in the reactor 1. In a preferred embodiment of the reactor 1, the diameter of the annular gap in the heating zone 4 is smaller than its diameter in the residence zone 5. The annular gap can also have different diameters within the heating zone 4.

[0060] In a preferred embodiment of reactor 1, the diameter of the annular gap in heating zone 4 is at most 30 mm, for example 25 mm or 20 mm or less, preferably 15 mm or 10 mm or less, and particularly preferably 4 to 6 mm or less. In a preferred embodiment of reactor 1, the annular gap in heating zone 4 has at least a portion a diameter of at most 30 mm, for example 25 mm or 20 mm or less, preferably 15 mm or 10 mm or less, and particularly preferably 4 to 6 mm or less. In a preferred embodiment of reactor 1, the diameter of the annular gap in heating zone 4 is at most 30 mm, for example 25 mm or 20 mm or less, preferably 15 mm or 10 mm, and particularly preferably 4 to 6 mm or less, and the compressed aqueous multicomponent mixture is heated in heating zone 4 by one or more heating elements. In the second pressure space 16 between the inner shell 2 and the outer shell 6 of reactor 1, the compressed aqueous multicomponent mixture is heated to 600 to 700 degrees Celsius as it flows through the annular gap. In a preferred embodiment of reactor 1, the annular gap of heating zone 4 has at least a diameter of up to 30 mm, for example 25 mm or 20 mm or less, preferably 15 mm or 10 mm or less, particularly preferably 4 mm to 6 mm or less, and the compressed aqueous multicomponent mixture is at least partially heated by one or more heating elements in the annular gap of heating zone 4. Heating elements are disposed in a second pressure space 16 between the inner shell 2 and the outer shell 6 of reactor 1, and the compressed aqueous multicomponent mixture is heated to 600 to 700 degrees Celsius as it flows through the annular gap of heating zone 4. For example, reactor 1 includes one, two, three, four, five, six, seven, eight, nine, ten or more, such as 14, 18, 20, 28, 30 or more heating elements, preferably electric heating elements, arranged in the second pressure space 16 surrounding the annular gap of heating zone 4.

[0061] Because the diameter of the annular gap in heating zone 4 is very small, or at least in a portion of heating zone 4, the flow rate of the compressed aqueous multicomponent mixture in this portion of heating zone 4 is very high. The dimensions of the annular gap in heating zone 4 are such that optimal heat transfer to the compressed aqueous multicomponent mixture is achieved. In different embodiments of reactor 1, the diameter of the annular gap, particularly the annular gap in heating zone 4, is adjusted according to the aqueous multicomponent mixture used as the reactant and the optimal heat transfer.

[0062] In heating zone 4, the diameter of the annular gap through which the compressed aqueous multicomponent mixture flows is relatively small, resulting in a large area for heat transfer to the compressed aqueous multicomponent mixture within heating zone 4, or at least in a portion thereof. This facilitates excellent heat transfer, enabling the flowing compressed aqueous multicomponent mixture to be rapidly and completely heated to up to 700 degrees Celsius, preferably up to 680 degrees Celsius. Corrosion of reactor 1 is minimized due to the high flow rate of the compressed aqueous multicomponent mixture in heating zone 4, or at least in a portion thereof. The flow rate of the compressed aqueous multicomponent mixture in heating zone 4 can be varied depending on the composition of the aqueous multicomponent mixture, the diameter of the annular gap, and the arrangement of the heating elements in heating zone 4.

[0063] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. The inner shell 2 contains a separation zone 3, which includes one or more heating elements for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius; and one or more separators for separating recyclable materials. The inner shell 2 also contains a heating zone 4 for heating the compressed aqueous multicomponent mixture after the recyclable materials have been separated to 600 to 700 degrees Celsius. The heating zone 4 includes a tubular heat exchanger WT5, a bypass, a heat exchanger WT4 10, and a bypass valve. The inner shell 2 also contains a residence zone 5 for supercritical hydrothermal gasification of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in a columnar shape, with the separation zone 3 located at the lower end of the column and the residence zone 5 located at the upper end. The heat exchanger WT4 10 is adjacent to the separation zone 3, and the tubular heat exchanger WT5 is connected to the bypass and heat exchanger WT4 10 on one side and to the residence zone 5 on the other side. Preferably, the tubular heat exchangers are arranged in the heating zone 4 as upright columns above the heat exchanger WT4 10.

[0064] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. A separation zone 3 within the inner shell 2 includes one or more heating elements for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius; and one or more separators for separating recyclable materials. Within the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multicomponent mixture after the recyclable materials have been separated to 600 to 700 degrees Celsius; the heating zone 4 includes a synthesis gas conduit 11. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal gasification of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in a columnar shape, with the separation zone 3 located at the lower end of the column and the residence zone 5 located at the upper end. The synthesis gas pipeline 11 is used to heat a portion of the compressed aqueous multi-component mixture in the heating zone 4, or to form an annular gap with the inner shell 2 throughout the heating zone 4. The synthesis gas pipeline 11 is connected to the bypass and heat exchanger WT4 10 on one side and to the residence zone 5 on the other side.

[0065] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. A separation zone 3 within the inner shell 2 includes one or more heating elements for heating the compressed aqueous multicomponent mixture to up to 550 degrees Celsius, and one or more separators for separating recyclable materials. Within the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multicomponent mixture after the recyclable materials have been separated to 600 to 700 degrees Celsius; the heating zone 4 includes a synthesis gas conduit 11. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in a columnar shape, with the separation zone 3 located at the lower end of the column and the residence zone 5 located at the upper end. The synthesis gas conduit 11 forms an annular gap with the inner shell 2 in a portion of or throughout the heating zone 4. An outer shell 6 surrounds the inner shell 2. A second pressure space 16 exists between the inner shell 2 and the outer shell 6. The second pressure space 16 includes a region in which one or more heating elements, preferably electric heating elements, are arranged for heating the compressed aqueous multicomponent mixture. This region surrounds the annular gap of the heating zone 4 for heating the compressed aqueous multicomponent mixture as it flows through the annular gap of the heating zone 4.

[0066] In a preferred embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. The inner shell 2 contains a separation zone 3, which includes one or more heating elements for heating the compressed aqueous multi-component mixture to 550 degrees Celsius, and one or more separators for separating recyclable materials. The inner shell 2 also contains a heating zone 4 for heating the compressed aqueous multi-component mixture after the recyclable materials have been separated to 600 to 700 degrees Celsius. The heating zone 4 includes a synthesis gas pipeline 11, a bypass, a heat exchanger WT4 10, and a bypass valve. The inner shell 2 also contains a residence zone 5 for supercritical hydrothermal gasification of the compressed aqueous multi-component mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in a columnar shape, with the separation zone 3 located at the lower end of the column and the residence zone 5 located at the upper end. In this reactor 1, the syngas conduit 11 forms an annular gap with the inner shell 2 for heating a compressed aqueous multicomponent mixture in a portion or the entire heating zone 4. An outer shell 6 surrounds the inner shell 2. A second pressure space 16 exists between the inner shell 2 and the outer shell 6. The second pressure space 16 includes a region where one or more heating elements, preferably electric heating elements, are arranged, surrounding the annular gap of the heating zone 4 for heating the compressed aqueous multicomponent mixture as it flows through the annular gap. A bypass and heat exchanger WT4 10 are preferably arranged above the separation zone 3 and connected to a heat exchanger or heat exchanger in the separation zone 3. In a preferred embodiment of the reactor 1, the syngas conduit 11 is arranged adjacent to the heat exchanger WT4 10 in the heating zone 4. The syngas conduit 11 is connected to the heat exchanger WT4 10 and the bypass. Supercritical water dissolved with syngas enters the heat exchanger WT4 10 and / or the bypass through the syngas conduit 11 and from there into the separation zone 3. In a preferred embodiment of reactor 1, the annular gap is arranged in the vertical column of heating zone 4, above heat exchanger WT4 10. Preferably, the bypass and heat exchanger WT4 10 are adjacent to each other in the vertical column. Preferably, the annular gap is arranged in the vertical column of heating zone 4, above the bypass and heat exchanger WT4 10.

[0067] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT3 13 and a separator A3 for heating the compressed aqueous multicomponent mixture to 300 degrees Celsius and separating the valuable material component WF3; a heat exchanger WT2 12 and a separator A2 for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius and separating the valuable material component WF2; and a heat exchanger WT1 9 and a separator A1 for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius and separating the valuable material component WF1. Within the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multicomponent mixture after the separation of recyclable materials to 600 to 700 degrees Celsius. The heating zone 4 includes a synthesis gas pipeline 11, a bypass, a heat exchanger WT4 10, and a bypass valve. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600-700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in an upright column. A synthesis gas conduit 11 forms an annular gap with the inner shell 2 within a portion or the entire heating zone 4. The diameter of the annular gap is less than 30 mm, preferably less than 20 mm. The annular gap in the upright column is located above the bypass and heat exchanger WT4 10. An outer shell 6 surrounds the inner shell 2. A second pressure space 16 exists between the inner shell 2 and the outer shell 6. The second pressure space 16 includes a region in which one or more electric heating elements are arranged, surrounding the annular gap of the heating zone 4, for heating the compressed aqueous multicomponent mixture as it flows through the annular gap of the heating zone 4.

[0068] In a preferred embodiment of reactor 1, the heating zone 4 is 2 to 10 meters long, preferably 3 to 5 meters. Preferably, reactor 1 includes an annular gap with a diameter less than 30 millimeters, for example, 25 or 20 millimeters or less, preferably 15 or 10 millimeters or less, and most preferably 4 to 6 millimeters or less. In a preferred embodiment of reactor 1, the heating zone 4 is 3 to 5 meters long and includes an annular gap. In a preferred embodiment of reactor 1, the heating zone 4 is 5 meters or less long, the annular gap has a diameter less than 30 millimeters, for example, 25 or 20 millimeters or less, preferably 15 or 10 millimeters or less, and includes a second pressure space 16, preferably including one or more electric heaters. In a preferred embodiment of reactor 1, the heating zone 4 is 3 to 5 meters long and includes a heat exchanger WT4 9 and an annular gap with a diameter of less than 20 mm or 15 mm, preferably 4 mm to 10 mm or less, arranged above the heat exchanger WT4 9. One or more heaters are arranged in the second pressure space 16 for heating the compressed aqueous multicomponent mixture in the annular gap.

[0069] In heating zone 4, the compressed aqueous multicomponent mixture is heated to 600 to 700 degrees Celsius, preferably approximately 600 to 700 degrees Celsius, for example, 570 degrees Celsius, 580 degrees Celsius, 590 degrees Celsius, 600 degrees Celsius, 610 degrees Celsius, 620 degrees Celsius, 630 degrees Celsius, 640 degrees Celsius, 650 degrees Celsius, 660 degrees Celsius, 670 degrees Celsius, 680 degrees Celsius, 690 degrees Celsius, 700 degrees Celsius, 705 degrees Celsius, and 710 degrees Celsius. For example, supercritical hydrothermal gasification can be carried out by adding a catalyst at a temperature below 600 to 700 degrees Celsius.

[0070] According to the present invention, the reactor 1 includes a residence zone 5 within an inner shell 2 for supercritical hydrothermal gasification of a compressed aqueous multicomponent mixture. The residence zone 5 is connected to a heating zone 4. The compressed aqueous multicomponent mixture, after being heated to 600 to 700 degrees Celsius, flows into the residence zone 5 and passes through it within 0.5 to 7 minutes, preferably 1 to 5 minutes, particularly 2 to 3 minutes. During this process, the compressed aqueous multicomponent mixture, or the organic compounds and organic components contained in the aqueous multicomponent mixture, are gasified under supercritical reaction conditions to form a syngas. In supercritical hydrothermal gasification, supercritical water serves as the reaction medium and as a reactant of the organic compounds and components contained in the aqueous multicomponent mixture. During supercritical hydrothermal gasification, these organic compounds and components are converted into a syngas. The syngas (= gasification product or product) is dissolved in the supercritical water 5 at a pressure of 25 to 35 MPa and a temperature present within the residence range.

[0071] The residence zone 5 is connected to the syngas conduit 11. In a particularly preferred embodiment of the reactor 1, the inner shell 2 of the residence zone 5 includes the syngas conduit 11. Preferably, the syngas conduit 11 is arranged within the residence zone 5. In this case, the syngas conduit 11 extends from the heating zone 4 into the residence zone 5, almost to the upper end of the residence zone 5, for example, to the upper third or upper quarter of the residence zone 5, preferably to the upper fifth or upper sixth of the residence zone 5, and especially preferably to the upper seventh or upper eighth of the residence zone 5. The upper end of the residence zone 5 is the portion of the residence zone 5 furthest from the heating zone 4. The end of the syngas conduit 11 has one or more openings at its upper end. Preferably, the syngas conduit 11 is open at its upper end. In a particularly preferred embodiment of the reactor 1, the inner shell 2 of the residence zone 5 includes the syngas conduit 11, which is open at one end extending into the residence zone 5. In a preferred embodiment of reactor 1, the inner shell 2 in the residence zone 5 has a tubular shape, with a corrugated bow at the end of the residence zone 5, and includes a synthesis gas conduit 11 inside the residence zone 5, extending at least to the upper third, preferably at least to the upper quarter, of the residence zone 5. The synthesis gas conduit 11 is connected to the residence zone 5 through an open end or one or more openings. In a particularly preferred embodiment of reactor 1, the inner shell 2 in the residence zone 5 includes the synthesis gas conduit 11, wherein the synthesis gas conduit 11 forms an annular gap with the inner shell 2 in a portion or the entire residence zone 5, the annular gap in the residence zone 5 having at least a diameter of at least 50 mm, and the synthesis gas conduit 11 has at least one opening in the residence zone 5 for introducing supercritical water dissolved in synthesis gas.

[0072] Due to the design and arrangement of the syngas conduit 11 in the heating zone 4 and the residence zone 5, the aqueous multicomponent mixture flows from the heating zone 4 to the residence zone 5. In a particularly preferred embodiment of reactor 1, the diameter of the syngas conduit 11 in the residence zone 5 is smaller than its diameter in the heating zone 4. In a particularly preferred embodiment of reactor 1, the diameter of the annular gap in the residence zone 5 is larger than its diameter in the heating zone 4. In a preferred embodiment of reactor 1, the diameter (annular gap) through which the compressible aqueous multicomponent mixture flows widens at the transition from the heating zone 4 to the residence zone 5, for example, the transition has a funnel shape, with the wide end of the funnel facing the residence zone 5. In a preferred embodiment of reactor 1, the diameter of the residence zone 5 is larger than the diameter of the heating zone 4. In a preferred embodiment of reactor 1, the diameter of the residence zone 5 is 2 meters or less, for example 1.5 meters or 1 meter, preferably 500 mm to 900 mm, more preferably 600 to 800 mm, for example 750 mm, 700 mm or 650 mm. In a preferred embodiment of reactor 1, the diameter of the annular gap in the residence zone 5 is 1 meter or less, for example, 700 mm or less, preferably 50 to 500 mm, for example, 100 to 400 mm, preferably 150 to 300 mm, for example, 150 mm, 200 mm, 250 mm, or 300 mm. In a preferred embodiment, the length of the residence zone 5 in reactor 1 is 0.5 m to 2 m, for example, 0.6 m to 1.8 m or 0.7 to 1.5 m, preferably 0.8 to 1.1 m. In a preferred embodiment of reactor 1, the inner shell 2 is tubular in shape within the residence zone 5, and the end of the residence zone 5 is corrugated.

[0073] The increased diameter of residence zone 5 reduces the flow rate of the compressed aqueous multicomponent mixture. In residence zone 5, the flow rate of the compressed aqueous multicomponent mixture approaches zero. Therefore, large hydrocarbons or hydrocarbons with strong bonds, such as long-chain hydrocarbons and aromatics, have a longer residence time than small and short-chain hydrocarbons. Through this design of reactor 1, supercritical hydrothermal gasification in the absence of oxygen is complete for all organic compounds contained in the compressed aqueous multicomponent mixture. The organic compounds contained in the compressed aqueous multicomponent mixture are converted into a syngas composed primarily or almost entirely of hydrogen, carbon dioxide, methane, and water. The syngas produced from the compressed aqueous multicomponent mixture by supercritical hydrothermal gasification has a lower density than the compressed aqueous multicomponent mixture and rises in residence zone 5 of the vertical column. In this case, the syngas is dissolved in supercritical water. The syngas dissolved in supercritical water is diverted at the upper end of residence zone 5 and flows into one or more openings of syngas conduit 11, the upper end of which includes one or more openings of residence zone 5.

[0074] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, there is a separation zone 3, which includes one or more heat exchangers and separators for heating a compressed aqueous multicomponent mixture to 550 degrees Celsius and separating recyclable materials. Within the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after separating the recyclable materials; the heating zone 4 includes a syngas conduit 11. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture, including the syngas conduit 11, after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in an upright column, with the separation zone 3 located at the lower end of the column and the residence zone 5 located at the upper end. The syngas conduit 11 forms an annular gap with the inner shell 2 in a portion of the heating zone 4 or in a portion of both the heating zone 4 and the residence zone 5. The diameter of the annular gap in the heating zone 3 is less than 30 mm, for example, 25 mm, 20 mm, or 15 mm or less, preferably 4 to 10 mm, while the diameter of the annular gap in the dwell zone 5 is 150 mm or more, preferably 200 to 300 mm. A synthesis gas pipe 11 is arranged in the dwell zone 5 and has at least one opening at its end, with the end of the synthesis gas pipe 11 located at the upper third of the dwell zone 5.

[0075] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT3 13 and a separator A3 for heating the compressed aqueous multicomponent mixture to 300 degrees Celsius and separating the valuable material component WF3; a heat exchanger WT2 12 and a separator A2 for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius and separating the valuable material component WF2; and a heat exchanger WT1 9 and a separator A1 for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius and separating the valuable material component WF1. Within the inner shell 2, a heating zone 4 is provided for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after separating the valuable fractions WF3, WF2, and WF1. The heating zone 4 includes a synthesis gas conduit 11, a bypass, a heat exchanger WT4 10, and a bypass valve. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of a compressed aqueous multicomponent mixture after heating to 600-700 degrees Celsius. The residence zone 5 includes a syngas pipeline 11. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in an upright column. The syngas pipeline 11 forms an annular gap with the inner shell 2 in a portion or throughout the heating zone 4. The diameter of the annular gap in the heating zone 4 is less than 20 mm, for example, 15 mm, or less than, for example, 10 mm. The annular gap in the heating zone 4 is arranged in and connected to the upright column above the bypass and heat exchanger WT4 10. The syngas pipeline 11 forms an annular gap with the inner shell 2 in a portion of the residence zone 5, and at least a portion of the annular gap in the residence zone 5 has a diameter of at least 150 mm. An outer shell 6 surrounds the inner shell 2. A second pressure space 16 exists between the inner shell 2 and the outer shell 6. The second pressure space 16 includes a region in which one or more electrically heated elements are arranged for heating the compressed aqueous multicomponent mixture to a supercritical hydrothermal vaporization temperature. This region surrounds an annular gap in the heating zone 4 and optionally extends at least partially into the residence zone 5. A synthesis gas conduit 11 extends at least into the upper third of the residence zone 5 and includes at least one opening in the residence zone 5. Preferably, at the transition from the heating zone 4 into the residence zone 5, the synthesis gas conduit 11 has a funnel shape, with the wider side of the funnel facing the residence zone 5.

[0076] In a preferred embodiment of the reactor 1 according to the invention, the arrangement, shape, and dimensions (diameter and length) of the heating zone 4, residence zone 5, and syngas conduit 11 in the column are selected in such a way that the compressed aqueous multicomponent mixture is heated to the temperature of supercritical hydrothermal vaporization, i.e., 600 to 700 degrees Celsius, as it flows through the heating zone 4, expands upon entering the residence zone 5, and resides for 0.5 to 7 minutes, preferably 1 to 5 minutes, for example, 2 to 3 minutes. Depending on the composition of the compressed aqueous multicomponent mixture, individual components contained in the compressed aqueous multicomponent mixture reside in the residence zone 5 for a longer or shorter time than other components. In the residence zone 5, the compressed aqueous multicomponent mixture undergoes hydrothermal vaporization under supercritical conditions to form syngas as a vaporization product, which dissolves in supercritical water under these pressure and temperature conditions. The supercritical water containing the dissolved syngas is directed to the syngas conduit 11 at the end of the residence zone 5. In a preferred embodiment, the inner shell 2 at the end of the residence zone 5 has a corrugated bow shape for this purpose.

[0077] In a preferred embodiment of reactor 1, a syngas conduit 11 is located within the residence zone 5 and the heating zone 4. In a preferred embodiment of reactor 1, the syngas conduit 11 begins inside the residence zone 5, below the upper end of the residence zone 4, for example below the corrugated bow, and is open at this end so that the generated syngas dissolved in the supercritical water flows into the syngas conduit 11 when reactor 1 is used as planned. In a preferred embodiment, reactor 1 includes a syngas conduit 11 with an open upper end, which is arranged within the inner shell 2 of reactor 1 in the residence zone 5 and passes through the residence zone 5 and the heating zone 4, wherein the diameter of the syngas conduit 11 increases (expands) as it enters the heating zone 4 from the residence zone 5.

[0078] In the intended use of reactor 1, syngas conduit 11 is used to pass supercritical water containing dissolved syngas through reactor 1. In the intended use, syngas conduit 11 also serves to separate the supercritical water containing dissolved syngas from a compressed aqueous multicomponent mixture flowing in the first pressure space 15 of the inner shell 2 of reactor 1, first through heating zone 4, and then into residence zone 5. In a particular embodiment of reactor 1, syngas conduit 11 introduces the supercritical water containing dissolved syngas into heat exchanger WT4 10, and optionally, through a bypass. In a particular embodiment of reactor 1, syngas conduit 11 introduces the supercritical water containing dissolved syngas into heat exchanger WT1 9. In a particularly preferred embodiment of reactor 1, syngas conduit 11 introduces the supercritical water containing dissolved syngas into a top heat exchanger within the column, such as heat exchanger WT4 10 or heat exchanger WT1 9. In a preferred embodiment of the reactor 1 according to the invention, the reactor 1 includes a heat exchanger WT4 10, a syngas pipeline 11 that opens into and connects to the heat exchanger WT4 10. Preferably, the syngas pipeline 11 opens into and connects to the heat exchanger WT4 10 with a bypass valve, the bypass being used to regulate the syngas flow rate and temperature in the heat exchangers WT4 10 and WT1 9. In a preferred embodiment of the reactor 1, a residence zone 5 is connected to the syngas pipeline 11, which causes the discharge of supercritical water dissolved in syngas and causes a compressed aqueous multicomponent mixture to be heated from the residence zone 5 first through the heating zone 4. The mixture then flows through the heat exchanger WT4 10 with the bypass valve, and through the bypass, through the heat exchanger WT1 9 into the separation zone 3, and if present, through the heat exchanger WT2 12, and if present, through the heat exchanger WT3 13, for discharging the supercritical water dissolved in syngas and heating the compressed aqueous multicomponent mixture. The compressed aqueous multicomponent mixture, flowing through the annular gap formed by the inner shell 2 and the syngas pipeline, is heated (heated) at the boundary with the syngas pipeline by supercritical water containing dissolved syngas, and at the boundary with the inner shell 2 by heating elements arranged in the second pressure space 16. This allows the compressed aqueous multicomponent mixture to be heated to the temperature of 600 to 700 degrees Celsius required for supercritical hydrothermal vaporization. In a preferred embodiment of reactor 1, the syngas pipeline 11 is a tubular heat exchanger WT5 and is connected to heat exchanger WT4 10 via a bypass valve and a bypass. In a preferred embodiment, the syngas pipeline 11 is connected to a bypass and a bypass valve. The syngas pipeline 11 can be a tubular heat exchanger WT5.

[0079] When reactor 1 is used as planned, the syngas conduit 11 is a device for countercurrent heating and compressing an aqueous multicomponent mixture with supercritical water. The syngas is dissolved in the supercritical water and is produced during supercritical hydrothermal vaporization, where the phases are immiscible. In this energy-advantageous process control, the heat from supercritical hydrothermal vaporization is used to heat the compressed aqueous multicomponent mixture (i.e., the fresh reactants). Simultaneously, this also cools the supercritical water containing the dissolved syngas. In a preferred embodiment of the invention, the temperature of the compressed aqueous multicomponent mixture entering the inner shell 2 of reactor 1 is approximately 100 degrees Celsius or lower, for example, 50 to 70 degrees Celsius, preferably 60 degrees Celsius, while the temperature of the water containing the dissolved syngas exiting the inner shell 2 is approximately 110 degrees Celsius or lower, for example, 60 to 80 degrees Celsius, preferably 70 degrees Celsius.

[0080] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, there is a separation zone 3, which includes one or more heat exchangers and separators for heating a compressed aqueous multi-component mixture to 550 degrees Celsius and for separating recyclable materials. Within the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multi-component mixture to 600 to 700 degrees Celsius after separating the recyclable materials; the heating zone 4 includes a syngas pipeline 11. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed aqueous multi-component mixture after heating to 600 to 700 degrees Celsius; the residence zone 5 includes the syngas pipeline 11. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in an upright column. The syngas pipeline 11 forms an annular gap with the inner shell 2 in a portion or throughout the heating zone 4. The syngas conduit 11 forms an annular gap with the inner shell 2 in part or all of the residence zone 5, and the annular gap in the residence zone 5 has at least a diameter of at least 150 mm. The syngas conduit 11 for introducing supercritical water in which the syngas is dissolved has at least one opening in the residence zone 5. The syngas conduit 11 for heating and compressing the aqueous multicomponent mixture passes through the heating zone 4 from the residence zone 5, and is connected to a heat exchanger WT4 10 with a bypass valve and bypass.

[0081] In a further embodiment of reactor 1 according to the invention, a syngas conduit 11 extends from heat exchanger WT410, passes through heat exchanger WT19, and if applicable, through heat exchanger WT212, and if applicable, through heat exchanger WT313, for heating a compressed aqueous multicomponent mixture to 550 degrees Celsius. In a further embodiment of reactor 1 according to the invention, syngas conduit 11 is connected to heat exchanger WT410, which is connected to heat exchanger WT19, which is connected to heat exchanger WT212, and which is connected to heat exchanger WT313, for heating the compressed aqueous multicomponent mixture with supercritical water in which syngas has been dissolved. In a further embodiment of reactor 1 according to the invention, syngas conduit 11 is connected to a bypass and heat exchanger WT410, which is connected to heat exchanger WT19, and which is connected to heat exchanger WT212. Heat exchanger WT2 12, connected to heat exchanger WT3 13, is used to heat a compressed water-based multicomponent mixture flowing countercurrently with supercritical water containing dissolved syngas. Syngas conduit 11 and the heat exchangers prevent mixing of the compressed water-based multicomponent mixture and the supercritical water containing dissolved syngas. Heat is transferred from the supercritical water containing dissolved syngas to the compressed water-based multicomponent mixture. The supercritical water containing dissolved syngas is cooled, while the compressed water-based multicomponent mixture is heated.

[0082] For example, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. In the inner shell 2, a separation zone 3 includes a heat exchanger WT3 13 and a separator A3 for heating the compressed aqueous multicomponent mixture to 300 degrees Celsius and separating the valuable material component WF3; a heat exchanger WT2 12 and a separator A2 for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius and separating the valuable material component WF2; and a heat exchanger WT1 9 and a separator A1 for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius and separating the valuable material component WF1. In the inner shell 2, there is a heating zone 4 for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after separating the valuable fractions WF3, WF2, and WF1. The heating zone 4 includes a synthesis gas pipeline 11, a bypass, a heat exchanger WT4 10, and a bypass valve. Within the inner shell 2, there is a residence zone 5 for heating a compressed aqueous multi-component mixture to 600-700 degrees Celsius for supercritical hydrothermal vaporization. This residence zone 5 includes a syngas conduit 11. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in an upright column. The syngas conduit 11 forms an annular gap with the inner shell 2 in a portion or the entire heating zone 4. The diameter of the annular gap in the heating zone 4 is less than 30 mm, preferably less than 20 mm or less than 10 mm. The annular gap in the upright column is located above the bypass and heat exchanger WT4 10. The syngas conduit 11 forms an annular gap with the inner shell 2 in part or the entire residence zone 5, and the annular gap in the residence zone 5 has at least a diameter of at least 150 mm. The syngas conduit 11, used to introduce supercritical water dissolved in syngas, has at least one opening in the residence zone 5. An outer shell 6 surrounds the inner shell 2. Between the inner shell 2 and the outer shell 6 is a second pressure space 16. The second pressure space 16 includes a region in which one or more electrically heated elements are arranged for heating the compressed aqueous multicomponent mixture to the temperature of supercritical hydrothermal vaporization, wherein this region of the pressure space 16 surrounds the annular gap of the heating zone 4. A synthesis gas conduit 11 for heating the compressed aqueous multicomponent mixture and cooling the supercritical water containing the synthesis gas is led out from the residence zone 5 through the heating zone 4, wherein the synthesis gas conduit 11 is connected to the heat exchanger WT4 10 and a bypass.

[0083] In a particularly preferred embodiment of the reactor 1 according to the invention, the separation zone 3, heating zone 4, and residence zone 5 are arranged in the form of vertical columns. The internal components of the reactor 1, particularly the separation zone 3, heating zone 4, residence zone 5, synthesis gas conduit 11, separators (A1, A2, A3), and heat exchangers (WT1, WT2, WT3, WT4, and possibly WT5), have a defined arrangement within the columns—as illustrated in the illustrative description of the various internal components of the reactor 1. Figures 1 to 4 As shown. In a preferred embodiment of reactor 1, separation zone 3 is arranged at the bottom of the vertical column, adjacent to heating zone 4, and adjacent to residence zone 5, within a compressible and sealable inner shell 2 at the top of the column. In a preferred embodiment of reactor 1, heat exchanger WT3 13 and separator A3 are arranged at the bottom of separation zone 3 of the vertical column, and heat exchanger WT2 12 and separator A2 are arranged above or adjacent to heat exchanger WT3 13 and separator A3. Heat exchanger WT1 9 and separator A1 are arranged above heat exchanger WT2 12 and separator A2, or above heat exchanger WT2 12 and separator A2, as well as heat exchanger WT3 13 and separator A3. In a preferred embodiment of reactor 1, heat exchanger WT4 10 and a bypass are arranged in the lower part of heating zone 4, which is adjacent to separator zone 3. Tubular heat exchanger WT5 or syngas pipe 11 and an annular gap are arranged in the upper and optional middle part of heating zone 4, which is adjacent to residence zone 5. In a preferred embodiment of reactor 1, heat exchanger WT3 13, separator A3, heat exchanger WT2 12, and separator A2 are arranged side-by-side in vertical columns in the lower layer of separator zone 3. Heat exchanger WT19 and separator A1 are arranged above heat exchanger WT2 12, separator A2, heat exchanger WT3 13, and separator A3. Heat exchanger WT19 is connected to heat exchanger WT2 12, and heat exchanger WT2 12 is connected to heat exchanger WT3 13, thereby compressing the aqueous multicomponent mixture.

[0084] The internal components, such as the inner shell 2, outer shell 6, heat exchanger, separator, syngas conduit 11, and heating elements, are arranged in a specific configuration within the column to separate recyclable materials, such as inorganic compounds, solids, sand, metals, metal salts, and nutrients like phosphates and ammonium, from a compressed aqueous multicomponent mixture via various thermal processes. For this purpose, the physical properties and equilibrium states between different phases are utilized, where the components of the compressed aqueous multicomponent mixture are located in different regions of the column. For example, in reactor 1 according to the invention, the two phases are in direct countercurrent contact at different locations within the column, or the liquid phase moves over the solid phase. For example, when reactor 1 is used as planned, different temperatures and flow rates exist in different regions of the column. When reactor 1 is used as planned, the flow types differ in different regions of the column; for example, turbulence is required in separation zone 3 to achieve good mixing and rapid heating. According to the present invention, the reactor 1 is cylindrical in shape, and the well-defined internal arrangement helps to increase mass and energy exchange and avoids backmixing of the separated recyclable materials and / or supercritical water (in which the synthesis gas is dissolved) with the compressed aqueous multicomponent mixture. Figures 1 to 4 A preferred embodiment of the reactor 1 according to the invention is shown, wherein the separation zone 3, the heating zone 4 and the residence zone 5 are a vertical column.

[0085] In a preferred embodiment of reactor 1, the compressible inner shell 2 has the form of a vertical column. When arranged as a vertical column, the residence zone 5 is preferably located at the upper part of the column, i.e., at the upper part of the compressible inner shell 2, the heating zone 4 is in the middle part of the column, and the separation zone 3 is in the lower part of the column. In a preferred embodiment, heat exchangers WT3 13 and separator A3 and heat exchangers WT2 12 and separator A2 are arranged side by side at the lower part of the column, i.e., on the same horizontal plane of the column, with heat exchanger WT19 and separator A1 arranged above them along the direction of the middle part of the column. In another preferred embodiment, heat exchangers WT3 13 and separator A3 are arranged at the lower part of the column, heat exchangers WT2 12 and separator A2 are arranged above them along the direction of the middle part of the column, and heat exchangers WT19 and separator A1 are arranged above them along the direction of the middle part of the column.

[0086] In other embodiments of reactor 1, heat exchanger WT1 9 and separator A1 are arranged either one on top of the other or side-by-side within the inner shell 2. In a particularly preferred embodiment of reactor 1, separator A1 is integrated into heat exchanger WT1 9 (heat exchanger with integrated separator WTA1 9'). In another embodiment of reactor 1, heat exchanger WT2 12 and separator A2 are arranged either one on top of the other or side-by-side. In a particularly preferred embodiment of reactor 1, separator A2 is integrated into heat exchanger WT2 12 (heat exchanger with integrated separator WTA2 12'). In another embodiment of reactor 1, heat exchanger WT3 13 and separator A3 are arranged either one on top of the other or side-by-side. In a particularly preferred embodiment of reactor 1, separator A3 is integrated into heat exchanger WT3 13 (heat exchanger with integrated separator WTA3 13'). A preferred embodiment of reactor 1 includes a heat exchanger with an integrated separator WTA1 9' as an internal component, or a heat exchanger with an integrated separator WTA2 12' if present, or a heat exchanger with an integrated separator WTA3 13 if present.

[0087] Known heat exchangers WT1 9, WT2 12, WT3 13, and WT4 10 can be used as heat exchangers, such as plate heat exchangers and tube bundle heat exchangers. The size and shape of the separation zone 3 and the heating zone 4 may need to be adjusted. According to the invention, a reactor with tubular heat exchangers WT1 9, WT2 12, WT3 13, and WT4 10 is used to heat a compressed aqueous multicomponent mixture to 600 or 700 degrees Celsius; for example, the length of the separation zone 3 and the heating zone 4 needs to be 30 to 40 meters. In the reactor with plate heat exchangers WT1 9, WT2 12, WT3 13, and WT4 10 according to the invention, heating a compressed aqueous multicomponent mixture to up to 600 or 700 degrees Celsius poses a risk of clogging at high flow rates.

[0088] In a particularly preferred embodiment of reactor 1, a pillow-plate heat exchanger is used as the heating element. In reactor 1 according to the invention, with pillow-plate heat exchangers WT1 9, WT2 12, WT3 13, and WT4 10, the heat exchangers can be arranged compactly. According to the invention, a reactor with pillow-plate heat exchangers WT1 9, WT2 12, and WT3 13, and optionally heat exchanger WT4 10, is used to heat compressed aqueous multicomponent mixtures to 600 or 700 degrees Celsius; for example, only 5 to 9 meters in length are needed in the separation zone 3 and heating zone 4. The pillow-plate heat exchanger has a characteristic pillow structure. Pillow-plate heat exchangers are particularly suitable for heating compressed aqueous multicomponent mixtures, such as biomass, wastewater, and sewage sludge. Due to the curved walls of the pillow-plate heat exchanger, a large amount of turbulence is generated even at low flow rates of the compressed aqueous multicomponent mixture; therefore, the compressed aqueous multicomponent mixture is uniformly and rapidly heated as it flows through the pillow-plate heat exchanger. Pillow plate heat exchangers also have high mechanical stability, thus reducing the risk of mechanical damage or deformation and the associated shutdown or necessary maintenance of reactor 1.

[0089] In a particularly preferred embodiment of reactor 1, heat exchanger WT1 9 is a pillow plate heat exchanger. In a particularly preferred embodiment of reactor 1, heat exchanger WT1 9 is a pillow plate heat exchanger, and heat exchanger WT4 10 is a pillow plate heat exchanger. In a particularly preferred embodiment of reactor 1 according to the invention, heat exchanger WT1 9 is a pillow plate heat exchanger, and heat exchanger WT2 12 is a pillow plate heat exchanger. In a particularly preferred embodiment of reactor 1 according to the invention, heat exchanger WT1 9 is a pillow plate heat exchanger, heat exchanger WT2 12 is a pillow plate heat exchanger, and heat exchanger WT4 10 is a pillow plate heat exchanger. In a particularly preferred embodiment of reactor 1 according to the invention, heat exchanger WT1 9 is a pillow plate heat exchanger, heat exchanger WT2 12 is a pillow plate heat exchanger, heat exchanger WT3 13 is a pillow plate heat exchanger, and heat exchanger WT4 10 is a pillow plate heat exchanger. In a particularly preferred embodiment, reactor 1 includes a pillow plate heat exchanger with integrated separators WTA1 9', WTA2 12', and WTA3 13'.

[0090] In a particularly preferred embodiment of reactor 1, separators A1, A2, and A3 are arranged one on top of another, with the heat exchangers rotated 90 degrees relative to each other. In a preferred embodiment, reactor 1 includes heat exchangers with integrated separators WTA1 9', WTA2 12', and WTA3 13', wherein the heat exchanger with integrated separator WTA1 9' is arranged above the heat exchangers with integrated separators WTA2 12' and WTA3 13', and the heat exchangers with integrated separators are rotated 90 degrees relative to each other. In a preferred embodiment, the heat exchangers are pillow-plate heat exchangers, with the separators integrated within them, arranged one on top of another, and the pillow-plate heat exchangers with integrated separators rotated 90 degrees relative to each other. Therefore, reactor 1 can be constructed compactly, allowing for the recovery of materials or valuable material components WF1, and, if applicable, the separation and removal of valuable material components WF2 and WF3 from reactor 1.

[0091] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger with an integrated separator WTA3 13' for heating the compressed aqueous multicomponent mixture to 300 degrees Celsius and separating the valuable material component WF1; a heat exchanger with an integrated separator WTA2 12' for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius and separating the valuable material component WF2; and a heat exchanger with an integrated separator WTA1 9' for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius and separating the valuable material component WF1. Within the inner shell 2, there is a heating zone 4 for heating the compressed water-based multicomponent mixture after separation of recyclable materials to 600 to 700 degrees Celsius. The heating zone 4 includes a synthesis gas conduit 11, a heat exchanger WT4 10, a bypass, and a bypass valve. Within the inner shell 2, there is a residence zone 5 for heating a compressed aqueous multi-component mixture to 600-700 degrees Celsius for supercritical hydrothermal vaporization. The residence zone 5 includes a syngas conduit 11. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in a vertical column. The syngas conduit 11 forms an annular gap with the inner sheath 2 in a portion or the entire heating zone 4. At least a portion of this annular gap in the heating zone 4 has a diameter less than 30 mm, preferably less than 20 mm or 10 mm or smaller. The syngas conduit 11 forms an annular gap with the inner shell 2 in part or the entire residence zone 5, and at least a portion of this annular gap in the residence zone 5 has a diameter of at least 150 mm. The syngas conduit 11, used to introduce supercritical water containing dissolved syngas, has at least one opening in the residence zone 5. An outer shell 6 surrounds the inner shell 2, and a second pressure space 16 exists between the inner shell 2 and the outer shell 6. The second pressure space 16 includes a region in which one or more electrically heated elements are arranged for heating the compressed aqueous multicomponent mixture to the temperature of supercritical hydrothermal vaporization. This region of the pressure space 16 surrounds an annular gap around the heating zone 4. A synthesis gas conduit 11 for heating the compressed aqueous multicomponent mixture and cooling the supercritical water passes through the heating zone 4 from the residence zone 5, and the synthesis gas conduit 11 is connected to the heat exchanger WT4 10 and a bypass.

[0092] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a pillow-plate heat exchanger with an integrated separator WTA3 13' for heating the compressed aqueous multicomponent mixture to a maximum of 300 degrees Celsius and separating the valuable material component WF1; a pillow-plate heat exchanger with an integrated separator WTA2 12' for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius and separating the valuable material component WF2; and a pillow-plate heat exchanger with an integrated separator WTA19' for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius and separating the valuable material component WF1. Within the inner shell 2, there is a heating zone 4 for heating the compressed water-based multicomponent mixture, after the separation of valuable material components WF3, WF2, and WF1, to 600-700 degrees Celsius. Heating zone 4 includes a pillow-plate heat exchanger WT410, a bypass valve, a bypass, and a synthesis gas pipeline 11. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed water-based multicomponent mixture after heating to 600-700 degrees Celsius. Residence zone 5 includes a synthesis gas pipeline 11. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in a columnar shape. An outer shell 6 surrounds the inner shell 2. Between the inner shell 2 and the outer shell 6 is a second pressure space 16. The second pressure space 16 includes a region in which one or more electric heating elements are arranged for heating the compressed water-based multicomponent mixture to the temperature for supercritical hydrothermal vaporization. This region of the pressure space 16 surrounds the annular gap of the heating zone 4. In this configuration, the syngas conduit 11 forms an annular gap with the inner shell 2 in a portion or the entire heating zone 4, the annular gap having at least a diameter of less than 30 mm, for example, less than 20 mm or less than 10 mm. The syngas conduit 11 also forms an annular gap with the inner shell 2 in a portion or the entire residence zone 5, the annular gap in the residence zone 5 having at least a diameter of at least 150 mm. The syngas conduit 11 for introducing supercritical water containing dissolved syngas has at least one opening in the residence zone 5. The syngas conduit 11 for heating and compressing the aqueous multicomponent mixture and cooling the supercritical water containing dissolved syngas exits from the residence zone 5 through the heating zone 4, and is connected to the pillow plate heat exchanger WT4 10 and a bypass. The pillow plate heat exchanger WT4 10 is connected to the pillow plate heat exchanger with integrated separator WTA1 9' in the bypass and separation zone 3. The pillow plate heat exchanger with integrated separator WTA1 9' is connected to the pillow plate heat exchanger with integrated separator WTA2 12'. The pillow plate heat exchanger with integrated separator WTA2 12' is connected to the column plate heat exchanger with integrated separator WTA3 13'.The separators of the pillow plate heat exchangers with integrated separators WTA1 9', WTA2 12', and WTA3 13' are arranged on top of each other. The pillow plate heat exchanger with integrated separator WTA2 12' is rotated 90 degrees relative to the pillow plate heat exchanger with integrated separator WTA3 13', and the pillow plate heat exchanger with integrated separator WTA1 9' is rotated 90 degrees relative to the pillow plate heat exchanger with integrated separator WTA2 12'. The internal components of the synthesis gas pipeline 11, pillow plate separator WT4 10, pillow plate heat exchangers with integrated separators WTA1 9', WTA2 12', and WTA3 13' are interconnected in this order, thus facilitating intended use. Supercritical water containing dissolved syngas flows sequentially through these internal components, thereby transferring heat to the compressed multi-component water mixture, which also flows through these internal components in a countercurrent flow to the supercritical water containing dissolved syngas, thus being heated to 600 to 700 degrees Celsius. The supercritical water containing dissolved syngas is separated from the compressed water-based multi-component mixture by the inner walls, so the compressed water-based multi-component mixture and the supercritical water containing dissolved syngas do not mix.

[0093] In a particularly preferred embodiment, the compressible sealable inner shell 2 of reactor 1 comprises a nickel-based alloy or a nickel-based superalloy or other suitable high-temperature and / or corrosion-resistant material. In another preferred embodiment, the compressible sealable inner shell 2 of reactor 1 comprises a nickel-based alloy or at least one nickel-based superalloy or other suitable high-temperature and / or corrosion-resistant material. In a particularly preferred embodiment, the materials of the internals arranged in the inner shell 2, such as heat exchangers WT1 9, WT2 12, WT3 13, WT4 10 and / or separators, such as separators A1, A2, A3 and / or heat exchangers with integrated separators, such as heat exchangers with integrated separators WTA1 9', WTA2 12', WTA3 13' and / or pillow plate heat exchangers, for example, pillow plate heat exchangers with integrated separators are made of nickel-based alloys. In another preferred embodiment, the materials of the internal components arranged in the inner shell 2 include nickel-based alloys or nickel-based superalloys or other suitable high-temperature and / or corrosion-resistant materials. For example, heat exchangers WT1 9, WT2 12, WT3 13, and WT4 9 in reactor 1 are composed of nickel-based alloys or nickel-based superalloys or other suitable high-temperature and / or corrosion-resistant materials. In another preferred embodiment, the materials of the separators, such as separators A1, A2, A3 and / or the materials of heat exchangers with integrated separators, such as heat exchangers with integrated separators WTA1 9', WTA2 12', and WTA3 13', include nickel-based alloys or nickel-based superalloys or other suitable high-temperature and / or corrosion-resistant materials. In another preferred embodiment, the materials of the pillow-plate heat exchangers, such as pillow-plate heat exchangers with integrated separators, include nickel-based alloys or nickel-based superalloys or other suitable high-temperature and / or corrosion-resistant materials. In a particularly preferred embodiment, reactor 1 includes a pillow plate heat exchanger and a pillow plate heat exchanger with integrated separators, for example, a pillow plate heat exchanger with integrated separators A1, A2, A3 and heat exchanger WT4 as a heating element, wherein all heat exchangers and separators are made of nickel-based alloy. In a particularly preferred embodiment, reactor 1 includes pillow plate heat exchangers WT1, WT2, WT3 and integrated separators A1, A2, A3 and heat exchanger WT4 as heating elements, wherein all heat exchangers and separators are made of nickel-based alloy.

[0094] Nickel-based alloys are materials whose main component is nickel, produced together with at least one other chemical element, typically through a melting process. Nickel-based alloys exhibit good corrosion resistance and / or high-temperature resistance (creep resistance). Nickel-based alloys include nickel-copper, nickel-iron, nickel-iron-chromium, nickel-chromium, nickel-molybdenum-chromium, nickel-chromium-cobalt, and other multi-material alloys. Most nickel-based alloys are classified according to international standards and are well known to those skilled in the art. In some embodiments of reactor 1, the inner shell 2, which can be sealed by pressure sealing, and the internal components within the inner shell 2, such as heat exchangers, separators, and syngas pipelines 11, are made of nickel-based alloys. In some embodiments of reactor 1, the compressible inner shell 2 and the internal components within the inner shell, such as heat exchangers, separators, and syngas pipelines 11, are composed of nickel-based alloys, wherein the compressible inner shell 2 and the internal components within the inner shell 2 may comprise, wholly or partially, further layers of other materials or materials.

[0095] In the reactor 1 according to the invention, the internal components arranged in the inner shell 2 of the reactor 1, such as heat exchangers WT19, WT2 12, WT3 13, WT4 10, separators A1, A2, A3, especially heat exchangers with integrated separators, particularly preferably pillow plate heat exchangers and pillow plate heat exchangers with integrated separators, have a wall thickness of less than 50 mm, for example 30 mm, for example 20 mm or 15 mm, preferably less than 10 mm, for example 5 mm. In a particularly preferred embodiment of the reactor 1, the internal components comprise thin, preferably thin, nickel-based alloy plates. For example, in some embodiments of the reactor 1, the wall thickness of the metal plates of the internal components is 10 mm or less, 5 mm or less, preferably 1 to 3 mm, less than 2 mm, particularly preferably about 1 mm, for example 1.5 to 0.75 mm. The thin wall thickness of the internal components, especially in the heat exchanger and syngas pipeline 11, results in very good heat transfer between the compressed aqueous multicomponent mixture and the supercritical water containing dissolved syngas in the separation zone 3 and the heating zone 4.

[0096] In the reactor 1 according to the invention, the wall thickness of the compressible sealable inner shell 2 of the reactor 1 is less than 50 mm, for example 30 mm or 20 mm or less, preferably 10 mm or less, for example 9 mm, 8 mm, 7 mm, 6 mm, 5 mm, 4 mm, 3 mm or less. In a particularly preferred embodiment, the compressible sealable inner shell 2 of the reactor 1 is made of a thin sheet of nickel-based alloy, for example, the wall thickness of the sheet of the inner shell 2 is 10 mm or less, 5 mm or less, preferably 1 to 3 mm, less than 2 mm, particularly preferably about 1 mm, for example 1.5 to 0.75 mm. Due to the extremely thin wall thickness of the inner shell 2, less nickel-based alloy is required during manufacturing, and very good thermal conductivity occurs between one or more heating elements arranged to heat the compressed aqueous multicomponent mixture to the supercritical hydrothermal vaporization temperature in the second pressure space 16, through which the compressed aqueous multicomponent mixture flows in the region surrounding the annular gap of the heating zone 4. One drawback of nickel-based alloys is that they have almost no compressive strength in temperature ranges above 550 degrees Celsius, particularly in the 600 to 700 degree Celsius range. If the inner shell 2 is thin-walled, the pressure difference between the pressure of the compressible aqueous multi-component mixture prevalent inside the inner shell 2 and the normal pressure outside the inner shell 2 will not be able to withstand it.

[0097] To ensure that there is no or only a small pressure difference between the interior (first pressure space 15) and the exterior of the compressible sealable inner shell 2, in a preferred embodiment, the reactor 1 includes a compressible sealable outer shell 6 surrounding the compressible sealable inner shell 2, and a second pressure space 16 is enclosed between the inner shell 2 and the outer shell 6. The pressure in the second pressure space 16 can be compressed, for example by a gas or liquid, to adapt to the pressure within the inner shell 2 during the intended operation of the reactor 1. In a preferred embodiment, the reactor 1 includes a second pressure space 16 located between the inner shell 2 and the outer shell 6, wherein the second pressure space 16 includes a gas, preferably an inert gas (inert gas) or a mixture of inert gases, compressible to a pressure of 25 to 35 MPa commonly present in the first pressure space 15. In other embodiments, the reactor 1 includes a liquid in the second pressure space 16 compressible to the pressure in the first pressure space 15.

[0098] An inert gas is a gas that is very inert under the relevant reaction conditions, or a gas that does not participate in or participates in only a few chemical reactions. In this document, an inert gas is defined as a gas that is very inert at pressures above 20 MPa, preferably between 25 and 35 MPa, and at temperatures between 200 and 700 degrees Celsius, and does not participate in or participates in only a very few chemical reactions. For example, elemental gases such as nitrogen, inert gases such as helium, neon, argon, krypton, and xenon, and gaseous molecular compounds such as sulfur hexafluoride and carbon dioxide can all be used as inert gases in the second pressure space 16. Furthermore, mixtures of the above gases can also be used. Suitable inert gases and gas mixtures are known to those skilled in the art.

[0099] In a preferred embodiment of reactor 1, the second pressure space 16 comprises nitrogen as an inert gas. In other preferred embodiments, the second pressure space 16 comprises a mixture of nitrogen and hydrogen, preferably a mixture with a hydrogen content ≤5 vol%. A nitrogen mixture with ≤5 vol% hydrogen is non-flammable. The nitrogen mixture with ≤5 vol% hydrogen may include other gaseous components, with the nitrogen content being at least 50 vol%. In the second pressure space 16, the mixture of nitrogen as a gas and ≤5 vol% hydrogen helps prevent scaling. Scaling is understood as the formation of a thick layer of oxidation products on the surface of a metallic material at high temperatures, a result of a metal-oxygen reaction.

[0100] In a preferred embodiment of the reactor 1 according to the invention, the pressure of the gas in the second pressure space 16 is matched with the pressure inside the inner shell 2. In a particularly preferred embodiment of the reactor 1, the metal sheet of the inner shell 2 comprises a nickel-based alloy with a wall thickness of less than 10 mm, preferably less than 5 mm, and particularly preferably less than 2 mm, and the pressure difference between the first pressure space 15 (pressure inside the inner shell 2) and the second pressure space 16 (pressure in the space between the inner shell 2 and the outer shell 6) is at most + / - 5 bar, that is, the pressure in the second pressure space 16 is at most 5 bar higher or at most 5 bar lower than the pressure in the first pressure space 15. Preferably, the pressure in the first pressure space 15 is higher than the pressure in the second pressure space 16, that is, preferably, the pressure in the first pressure space 15 is at most 5 bar higher than the pressure in the second pressure space 16. For example, the pressure inside the sealable inner shell 2 is 27.3 MPa, and the pressure inside the second pressure space 16 is 27 MPa. This avoids the pressure difference between the first pressure space 15 and the second pressure space 16 inside the inner shell 2 exceeding 5 bar. The inner shell 2, made of a nickel-based alloy, has a wall thickness of less than 10 mm, preferably less than 5 mm, and especially preferably less than 2 mm, so that it is exposed to little or no pressure differential.

[0101] In a particularly preferred embodiment of reactor 1, the metal plate of the inner shell 2 comprises a nickel-based alloy with a wall thickness of less than 10 mm, preferably less than 5 mm, and particularly preferably less than 2 mm. The pressure difference between the first pressure space 15 (pressure within the inner shell 2) and the third pressure space 17 (pressure within the heat exchanger and the syngas pipeline 11) is at most + / - 2 bar, preferably + / - 1 bar or less, and particularly preferably + / - 0.5 bar, + / - 3 bar, + / - 0.1 bar or less. Internal components arranged within the inner shell 2, such as the heat exchanger, separator, bypass, and syngas pipeline, are also made of a nickel-based alloy with a wall thickness of less than 10 mm, preferably less than 5 mm, and particularly preferably less than 2 mm, thus avoiding contact with or only contacting very small pressure differences.

[0102] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT1 9 and a separator A1 for heating a compressed aqueous multicomponent mixture to a maximum of 550 degrees Celsius and separating the valuable material component WF1 from the compressed aqueous multicomponent mixture. Within the inner shell 2, a heating zone 4 is provided for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the valuable material component WF1 has been separated. The heating zone 4 includes a syngas pipeline 11, a bypass, and a heat exchanger WT4. Within the inner shell 2, a residence zone 5 is provided for supercritical hydrothermal gasification of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The residence zone 5 includes the syngas pipeline 11. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in a vertical column. The inner shell 2, heat exchanger WT1 9, heat exchanger WT4 10, separator A1 and synthesis gas pipeline 11 are made of nickel-based alloy or have a wall thickness of 500 mm or less, preferably 200 mm or less.

[0103] In a further embodiment, the reactor 1 according to the invention includes an inner shell 2, which can be sealed by pressure sealing. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT1 9 and a separator A1 for heating a compressed aqueous multicomponent mixture to a maximum of 550 degrees Celsius and separating the valuable material component WF1 from the compressed aqueous multicomponent mixture. Within the inner shell 2, a heating zone 4 is provided for heating the compressed aqueous multicomponent mixture after the separation of recyclable materials to 600 to 700 degrees Celsius; the heating zone 4 includes a syngas pipeline 11, a bypass, and a heat exchanger WT4. Within the inner shell 2, a residence zone 5 is provided for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius; the residence zone 5 includes the syngas pipeline 11. A compressible outer shell 6 surrounds the inner shell 2. A second pressure space 16 exists between the inner shell and the outer shell. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in an upright column. The inner shell 2, heat exchangers WT1 9, WT4 10, separator A1, and synthesis gas pipeline 11 are made of nickel-based alloys or have a wall thickness of 10 mm or less, preferably 5 mm or less. The second pressure space 16 contains a compressible inert gas or liquid.

[0104] In a further embodiment, the reactor 1 according to the invention comprises a pressurizable inner shell 2 that encloses a first pressure space 15. Within the inner shell 2, a separation zone 3 comprises a pillow-plate heat exchanger with an integrated separator WTA3 13' for heating a compressed aqueous multicomponent mixture to a maximum of 300 degrees Celsius and separating the valuable material component WF1; a pillow-plate heat exchanger with an integrated separator WTA2 12' for heating the compressed aqueous multicomponent mixture to 400 degrees Celsius and separating the valuable material component WF2; and a pillow-plate heat exchanger with an integrated separator WTA19' for heating the compressed aqueous multicomponent mixture to 550 degrees Celsius and separating the valuable material component WF1. Within the inner shell 2, there is a heating zone 4 for heating the compressed water-based multi-component mixture after the separation of valuable material components WF3, WF2, and WF1 to 600-700 degrees Celsius. Heating zone 4 includes a pillow-plate heat exchanger WT4 10, a bypass valve, a bypass, and a syngas pipeline 11. Within the inner shell 2, there is a residence zone 5 for supercritical hydrothermal vaporization of the compressed water-based multi-component mixture after heating to 600-700 degrees Celsius. Residence zone 5 includes the syngas pipeline 11. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in an upright column. The syngas pipeline 11 forms an annular gap with the inner shell 2 in a portion or throughout the heating zone 4. At least a portion of the annular gap has a diameter of at most 30 mm or less, preferably 20 mm or 15 mm or less, for example, 4 to 10 mm. In this configuration, the syngas conduit 11 forms an annular gap with the inner shell 2 in a partial or complete residence zone 5, and the annular gap in the residence zone 5 has at least a diameter of at least 150 mm. The syngas conduit 11, used for introducing supercritical water dissolved in the syngas, has at least one opening in the residence zone 5. An outer shell 6 surrounds the inner shell 2. A second pressure space 16 exists between the inner shell 2 and the outer shell 6. The second pressure space 16 includes a region in which one or more electrically heated elements are arranged for heating a compressed aqueous multicomponent mixture to the temperature of supercritical hydrothermal vaporization, and this region of the pressure space 16 surrounds the annular gap of the heating zone 4. The second pressure space 16 comprises a compressible inert gas or a compressible liquid, and the pressure difference between the first pressure space 15 and the second pressure space 16 is at most + / - 5 bar. Various techniques for setting the pressure of the inert gas or compressible liquid in the second pressure space 16 are known to those skilled in the art.

[0105] By matching the pressure of the second pressure space 16 with the pressure of the first pressure space 15 (pressure within the inner shell 2) and / or the pressure of the third pressure space 17 (pressure within the heat exchanger and synthesis gas pipeline 11), the pressure load on the inner shell 2 and the pressure load on the internal components are minimized or eliminated. Therefore, the nickel-based alloy material is exposed to high temperatures in the residence and heating zones 4, but with little or no pressure load. Thus, high-quality materials, such as nickel-based alloys, with high temperature and corrosion resistance but only low pressure resistance, can be used for the thin walls of the inner shell 2 and the internal components within it. Since temperature- and corrosion-resistant materials such as nickel-based alloys are very expensive, these embodiments of reactor 1 reduce the material cost of manufacturing reactor 1. Due to the pressure release of the inner shell 2 and the internal components located within it, the nickel-based alloy walls can be made very thin. Therefore, the required material is significantly reduced. The investment in reactor 1 is reduced to approximately one-eighth of the material cost required without pressure release. Since the reactor 1 according to the invention is significantly lighter in this embodiment due to the thinner walls of the inner shell 2, transportation and maintenance costs are also reduced, in addition to manufacturing costs.

[0106] In a preferred embodiment of the reactor 1 according to the invention, the distance between the pressure-resistant sealing inner shell 2 and the pressure-resistant sealing outer shell 6 is at least 100 mm, preferably at least 150 mm, and particularly preferably at least 200 mm or more. In other embodiments of the reactor 1, the distance between the compressible sealing inner shell 2 and the compressible sealing outer shell 6 is not always the same. In a preferred embodiment of the reactor 1 according to the invention, at least in the residence zone 5 and optionally in at least part of the heating zone 4 arranged in the inner shell 2, the distance between the compressible sealing inner shell 2 and the compressible sealing outer shell 6 is at least 100 mm, preferably at least 150 mm, and particularly preferably at least 200 mm or more.

[0107] In a preferred embodiment of the reactor 1 according to the invention, the second pressure space 16 comprises at least one layer of thermal insulation material, preferably one or more high-temperature insulation layers. In a preferred embodiment of the reactor 1 according to the invention, the second pressure space 16 comprises two layers of insulation material, preferably two high-temperature insulation layers. For example, the first and second insulation layers may have different thermal conductivities. Preferably, the first and second insulation layers have different heat transfer coefficients. Preferably, the first and second insulation layers have different thermal conductivities and different heat transfer coefficients. Preferably, the first and second insulation layers are bonded together. The insulation layers comprise or consist of insulation material, preferably high-temperature insulation layers. In the reactor 1 according to the invention, the insulation material of the insulation layers can be independently selected from high-temperature wool, mineral wool, ceramic wool, and mineral insulating materials. Other suitable insulation materials are known to those skilled in the art.

[0108] One or more insulation layers may completely or partially surround the inner shell 2. In one embodiment of reactor 1, the insulation layer completely surrounds the inner shell 2 except for the bottom-facing portion. In another embodiment, the insulation layer completely surrounds the inner shell 2 except for the bottom plate 7. In a further preferred embodiment of reactor 1, at least the area of ​​residence zone 5 located within the inner shell 2 is surrounded by one or more thermal insulation layers. In a further preferred embodiment of reactor 1, at least inside the inner shell 2, the area containing residence zone 5 and heating zone 4 is surrounded by one or more insulation layers.

[0109] In a preferred embodiment of the reactor 1 according to the invention, the distance between the inner shell 2 and the outer shell 6 is at least 100 mm, preferably at least 150 mm, particularly preferably at least 200 mm or more, and this area includes one or two layers of insulation material. In another preferred embodiment of the reactor 1 according to the invention, at least in the area where the heating zone 4 is arranged in the inner shell 2, the distance between the inner shell 2 and the outer shell 6 is at least 100 mm, preferably at least 150 mm, particularly preferably at least 200 mm or more, and this area includes one or two layers of insulation material. In the reactor 1 according to the invention, the thickness of the first layer of insulation material can be at least 25 mm, preferably at least 40 mm, more preferably at least 50 mm or more. In the reactor 1 according to the invention, the thickness of the second layer of insulation material can be at least 80 mm, preferably at least 100 mm, more preferably at least 150 mm or more.

[0110] In a preferred embodiment of the reactor 1 according to the invention, the distance between the inner shell 2 and the outer shell 6 is 200 mm, and this area includes a first layer of thermal insulation material with a thickness of 50 mm and a second layer of thermal insulation material with a thickness of 150 mm. In a preferred embodiment of the reactor 1 according to the invention, the distance between the inner shell 2 and the outer shell 6 is 100 mm, and this area includes a first layer of thermal insulation material with a thickness of 50 mm and a second layer of thermal insulation material with a thickness of 50 mm.

[0111] In other preferred embodiments of the reactor 1 according to the invention, at least in the area where the residence zone 5 and (if appropriate) at least partially the heating zone 4 are arranged in the inner shell 2, the distance between the inner shell 2 and the outer shell 6 is at least 200 mm, and this area includes a layer of thermal insulation material with a thickness of 50 mm and a second layer of thermal insulation material with a thickness of 150 mm. In other preferred embodiments of the reactor 1 according to the invention, at least in the area where the residence zone 5 and optionally at least partially the heating zone 4 are arranged in the inner shell 2, the distance between the inner shell 2 and the outer shell 6 is at least 100 mm, and this area includes a layer of thermal insulation material with a thickness of 50 mm or more and a second layer of thermal insulation material with a thickness of 50 mm or more.

[0112] In a particularly preferred embodiment of reactor 1, the second pressure space 16 comprises an inert gas and two layers of insulation material. Although the temperature of the residence zone 5 of the inner shell 2 is 600 to 700 degrees Celsius during supercritical hydrothermal gasification, the temperature of the compressible outer shell 6 is only 350 degrees Celsius or lower, preferably 300 degrees Celsius or 280 degrees Celsius or lower, most preferably 200 degrees Celsius or lower. Depending on the embodiment of reactor 1, whether using an inert gas or a compressible liquid, the thickness and material of the first insulation layer (if applicable), and the thickness and material of the second insulation layer (if applicable), the temperature inside the pressure-sealed outer shell 6 is between 100 and 250 degrees Celsius, for example, 220 degrees Celsius, 200 degrees Celsius, 150 degrees Celsius or lower. These temperature specifications for the interior of the outer shell 6 refer to the area of ​​the residence zone 5 located inside the inner shell 2.

[0113] In a particular embodiment, the reactor 1 according to the invention includes a conduit 14 for adding a precipitant to the separation zone 3, for example for adding a precipitant such as Mg. 2+ Ca 2+ and K + The precipitant is added to a compressed aqueous multicomponent mixture. Reactor 1 may include, for example, a conduit 14 for adding a precipitant in separation zone 3, the arrangement of which allows the precipitant to be added to the compressed aqueous multicomponent mixture before the valuable fraction WF1 is separated at 550°C, preferably 400 to 550°C, to achieve the most complete separation of phosphate and ammonium in separation zone 3. In a preferred embodiment, reactor 1 according to the invention includes a conduit 14 for adding the precipitant, which is connected to a heat exchanger WT1 9 and / or separator A1. In a preferred embodiment, reactor 1 according to the invention includes a conduit 14 for adding the precipitant, which is connected to a heat exchanger with an integrated separator WTA1 9'. In a preferred embodiment, reactor 1 according to the invention includes a conduit 14 for adding the precipitant, which leads to separator A1 or the integrated separator.

[0114] In a particularly preferred embodiment, the inner shell 2 includes an opening that can be closed by compression using the base plate 7. In a particularly preferred embodiment, both the inner shell 2 and the outer shell 6 include an opening that can be closed by pressure sealing using the base plate 7. Compressible sealing means that when the inner shell 2 and the outer shell 6 are compressed and sealed, a set pressure of approximately 25 to 35 MPa is maintained in the first pressure space 15 and the second pressure space 16. In a particular embodiment, the outer shell 6 includes an opening that can be compressed and sealed using the base plate 7.

[0115] In a preferred embodiment, reactor 1 includes an opening in the inner shell 2 for a bottom plate and a bottom plate 7 pressurized to the pressurized and sealable inner shell 2. In a preferred embodiment, reactor 1 includes an opening in the bottom plate in the inner shell 2 and outer shell 6, and a bottom plate 7 pressurized to the pressurized and sealable inner shell 2 and pressurized and lockable outer shell 6. In a preferred embodiment, a heat exchanger and a separator in the inner shell 2 are arranged on the bottom plate 7. A separator region 3 is adjacent to the bottom plate 7. In a preferred embodiment, the separator region 3, heating region 4, and residence region 5 are arranged on the bottom plate 7 as uprights within the inner shell 2, the inner shell 2 being pressure-sealed to the bottom plate 7. Preferably, in this embodiment of reactor 1, the separation region 3 is arranged above the bottom plate 7, the residence region 5 is located at the uppermost part of the inner shell 2, and the heating region 4 is located between the separation region 3 and the residence region 4, wherein the separation region 3 is adjacent to the heating region 4, and the heating region 4 is adjacent to the residence region 5. In a preferred embodiment, reactor 1 according to the invention includes a bottom plate 7 made of steel. In a preferred embodiment, the reactor 1 according to the invention includes a bottom plate 7 with a thickness of 20 cm or less, such as 15 cm or 10 cm.

[0116] In a preferred embodiment, the reactor 1 according to the invention comprises a compressible, sealable inner shell 2 surrounding a first pressure space 15 and having an opening for a bottom plate 7. Within the inner shell 2, a separation zone 3 includes a heat exchanger WT1 9 and a separator A1 for heating the compressed aqueous multicomponent mixture to a maximum of 550 degrees Celsius and separating the valuable material component WF1 from the compressed aqueous multicomponent mixture. In the heating zone 4 within the inner shell 2, one or more heating elements are provided for heating the compressed aqueous multicomponent mixture to 600 to 700 degrees Celsius after the valuable material component WF1 has been separated. A residence zone 5 within the inner shell 2 is provided for supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture after heating to 600 to 700 degrees Celsius. The separation zone 3, heating zone 4, and residence zone 5 are interconnected and arranged in an upright column on the bottom plate 7. The bottom plate 7 is connected to the inner shell 2 by a flange and is pressed and sealed. The separation zone 3 is arranged above the bottom plate 7, the heating zone 4 is arranged above the separation zone 3, and the dwell zone 5 is arranged above the heating zone 4.

[0117] In a preferred embodiment, reactor 1 includes a base plate 7 having one or more openings through a conduit 14, such as one or more openings for introducing a compressed aqueous multicomponent mixture into a reactant line of the inner shell 2, wherein the reactant line is connected to the base plate 7 in a compressible seal. In a preferred embodiment, reactor 1 according to the invention includes a base plate 7 having at least one opening for separating recyclable materials. In a preferred embodiment, reactor 1 includes at least one opening of conduit 14 for separating valuable material component WT1, optionally with a valve. In a preferred embodiment, reactor 1 includes at least one opening of conduit 14, optionally with a valve for separating valuable material component WT1, and at least one opening of conduit 14, optionally with a valve for separating valuable material component WT2. In a preferred embodiment, reactor 1 includes at least one optional opening of conduit 14 for separating valuable material component WT1, at least one optional opening of conduit 14 for separating valuable material component WT2, and at least one optional opening of conduit 14 for separating valuable material component WT3. Each conduit 14 for separating recyclable or valuable material components is compressibly connected to the base plate 7. In a preferred embodiment, the reactor 1 according to the invention includes a base plate 7 with at least one opening for a syngas conduit 11 for separating water containing syngas (i.e., cooled supercritical water previously dissolved with syngas), the conduit being pressurized and lockable to the base plate 7. In a preferred embodiment, the reactor 1 according to the invention includes a base plate 7 having one or more openings for connection to one or more gas conduits in a second pressure space 16 for introducing gas or liquid and regulating the pressure in the second pressure space 16, each gas conduit being compressibly connected to the base plate 7. In a preferred embodiment, the reactor 1 according to the invention includes a base plate 7 having at least one opening for a conduit 14 for adding precipitate, wherein the conduit 14 for adding precipitate is pressure-sealed to the base plate 7 and connected to a first pressure space 15.

[0118] In a preferred embodiment of reactor 1, the bottom plate 7 is connected to the compressible inner shell 2 via a flange connection. In another preferred embodiment of reactor 1, the bottom plate 7 is connected to the compressible outer shell 6 via a flange connection. Suitable flange connections allow for a pressure-sealed connection between the inner shell 2 and the bottom plate 7, and, if applicable, between the outer shell 2 and the bottom plate 7. The flange connections also allow the inner shell 2 and, if applicable, the outer shell 6 to be removed for replacement or servicing of internal equipment, such as heat exchangers or other heating elements, separators, syngas piping 11, bypass valves, or for cleaning of the inner shell 2 or its internal equipment. Suitable flange connections are known to those skilled in the art, for example, as disclosed in EP1010931B1.

[0119] In a preferred embodiment of reactor 1, the outer shell 6 is made of steel, preferably high-strength steel, such as stainless steel. In certain embodiments, the outer shell 6 is made of a steel coating, for example, the outer shell 6 includes a fiberglass layer, for example, the outer shell 6 includes a fiberglass layer on the outside. For example, the wall thickness of the outer shell 6 is 150 mm or less, such as 90 mm or 50 mm. In a preferred embodiment of reactor 1, the outer shell 6 is made of steel with a wall thickness of 80 mm or less.

[0120] In a preferred embodiment of reactor 1, the diameter of the outer shell 6 is 5 meters or less, preferably 3 meters or 1 meter, more preferably 2 to 1.5 meters, 1.9 to 1.6 meters, 1.7 meters or 1.8 meters. In a preferred embodiment, the outer shell 6 is cylindrical.

[0121] In a preferred embodiment, reactor 1 includes a steel frame 8 that surrounds and stabilizes the outer shell 6. In a preferred embodiment, reactor 1 according to the invention is stabilized by steel scaffolding 8. Preferably, the steel scaffolding 8 surrounds the outer shell 6. In a preferred embodiment, the steel scaffolding 8 extends onto and optionally connects to a base plate 7. Preferably, the steel scaffolding 8 surrounding and stabilizing the reactor extends to the ground. For example, the steel scaffolding 8 is connected to a foundation on the ground.

[0122] To allow for pressure adjustment in the second pressure space 16, the outer shell 6 can be closed by compression. The inner shell 2 can be pressurized to maintain pressure in the first pressure space 15 during and after the heating and compression of the aqueous multicomponent mixture, the separation of recyclable or valuable material components from the compressed aqueous multicomponent mixture, further heating and compression of the aqueous multicomponent mixture, and during and after the supercritical hydrothermal vaporization of the compressed aqueous multicomponent mixture. When the reactor 1 is used as planned, the outer shell 6 and the inner shell 2 are sealed by pressure. When the reactor 1 is used as planned, the pressure in the second pressure space 16 is adjusted, and the inert gas or compressible liquid within the second pressure space 16 is compressed. The pressure within the inner shell 2 is transferred from the inner shell 2 to the outer shell 6 of the reactor 1 via the compressed inert gas or liquid. The pressure of the compressed inert gas or liquid in the second pressure space 16 acts on the outer wall of the inner shell 2, while the pressure of the compressed aqueous multicomponent mixture acts on the inner wall of the inner shell 2. Therefore, pressure acts on the surface of the inner shell 2 from two directions, preventing damage or deformation of the inner shell 2 due to large pressure differences and ensuring the mechanical stability of the inner shell 2. In the case of compressing inert gas, this achieves pneumatic compression of the inner shell 2; in the case of compressing liquid, it achieves hydraulic compression of the inner shell 2. During the start-up (commissioning) of reactor 1, the inner shell 2 is filled with an aqueous multi-component mixture compressed to 25 to 35 MPa. The temperature in the heating element of the separation zone is raised to 550 degrees Celsius, and the temperature in the heating element of the heating zone and the heater of the second pressure space 16 is raised to 600 to 700 degrees Celsius. Simultaneously, the pressure inside the inner shell 2 increases. When reactor 1 starts up, the pressure inside the outer shell 6 also increases according to the pressure inside the inner shell 2. During the specified operation, the pressure in the second pressure space 6 is adjusted to match the pressure inside the inner shell 2 to avoid a pressure difference greater than 5 bar.

[0123] Reactor 1 is preferably operated as a flow-through reactor. When reactor 1 according to the invention is operated as planned, inert gas is introduced into the second pressure space 16 through a first gas conduit, which is pressure-sealed to the outer shell 6 via a base plate 7. When reactor 1 according to the invention is operated as planned, inert gas is discharged from the second pressure space 16 through a second gas conduit, which is pressure-sealed to the outer shell 6 via the base plate 7. When reactor 1 according to the invention is operated as planned, a compressed aqueous multi-component mixture is introduced into the inner shell 2 of reactor 1 through a reactant conduit, which is pressure-sealed to the inner shell 2 via the base plate 7. When reactor 1 according to the invention is operated as planned, water-soluble synthesis gas is discharged from the inner shell 2 of reactor 1 through a synthesis gas conduit 11, which is pressure-sealed to the inner shell 2 via the base plate 7. The pressure in the second pressure space 16 is regulated according to known procedures using high-pressure gas tanks, low-pressure gas tanks, and, if necessary, medium-pressure gas tanks. The corresponding procedures are known to those skilled in the art.

[0124] Another object of the present invention is to provide a method for manufacturing reactor 1 according to the present invention.

[0125] One object of the present invention is an apparatus for operating a reactor 1 according to the invention, comprising the reactor 1 according to the invention and one or more pumps. A preferred embodiment of the apparatus for operating the reactor 1 according to the invention includes a high-pressure pump for compressing an aqueous multicomponent mixture to 25 to 35 MPa. For example, the high-pressure pump is located below or to one side of the base plate 7.

[0126] One embodiment of the apparatus for operating the reactor 1 according to the invention includes the reactor 1 according to the invention, a high-pressure pump for compressing the aqueous multi-component mixture to 25 to 35 MPa, and a shredding device. Another embodiment of the apparatus for operating the reactor 1 according to the invention includes the reactor according to the invention, a high-pressure pump for compressing the aqueous multi-component mixture to 25 to 35 MPa, a shredding device for pulverizing the multi-component mixture used as a reactant, and a device for diluting the multi-component mixture used as a reactant. According to the invention, the apparatus for operating the reactor 1 preferably includes a circulating water pipeline for diluting the multi-component mixture used as a reactant with (process) water, for example, water obtained by expanding a syngas-water mixture (a product of supercritical hydrothermal gasification).

[0127] A preferred embodiment of the apparatus for operating reactor 1 according to the invention preferably includes means for measuring and regulating the gas pressure in the second pressure space 16. In one embodiment, the system for operating reactor 1 according to the invention includes a low-pressure gas storage tank for an inert gas and a high-pressure gas storage tank for an inert gas. The low-pressure and high-pressure gas storage tanks are connected to the second pressure space 16 of reactor 1 according to the invention, for example, via gas pipelines. The gas pressure in the second pressure space 16 can be regulated by the low-pressure and high-pressure gas storage tanks. In one embodiment, the apparatus for operating reactor 1 according to the invention includes a low-pressure gas storage tank for an inert gas, a high-pressure gas storage tank for an inert gas, and a medium-pressure gas storage tank for an inert gas. In one embodiment, the system for operating reactor 1 according to the invention preferably includes one or more gas pipelines and valves for regulating the inert gas pressure in the second pressure space 16, preferably at least one pressure measuring device, and optionally a temperature measuring device, which are connected to the second pressure space 16.

[0128] According to the present invention, a preferred embodiment of the apparatus for operating reactor 1 includes a pump for pumping precipitate through precipitate line 14 into separation zone 3 of inner shell 2. For example, the pump for pumping precipitate is arranged below or from the side of bottom plate 7 and connected to separation zone 3 via line 14.

[0129] According to the invention, a preferred embodiment of the equipment for operating reactor 1 includes a container connected to reactor 1 according to the invention. Another preferred embodiment of the equipment for operating reactor 1 according to the invention includes a container comprising electronic infrastructure for controlling reactor 1, including (if appropriate) connections to a control system and gas supply, including (if appropriate) connections to a control system and power supply, including (if appropriate) connections to a control system and a cooling system for separating water from the syngas-water mixture, and (if appropriate) other components. In this way, a fully designed plant can be manufactured, delivered, and rapidly put into operation.

[0130] A plant including the reactor 1 according to the invention is, for example, a waste treatment plant, a water treatment plant, or a power supply plant. A specific embodiment of the plant includes the reactor 1 according to the invention. A container includes electronic infrastructure for controlling the reactor 1, preferably a connection to a gas supply, preferably a connection to a power source, preferably a cooling connection, preferably a pipeline connection, preferably a product connection, and preferably a connection to recyclable materials, wherein the electronic infrastructure is connected to the reactor via electrical wires, and if present, the aforementioned connections are connected to the reactor via corresponding lines. Optionally, a pulverizing device for pulverizing the multi-component mixture as reactants is connected to the reactant pipeline. Optionally, a dilution device for diluting the multi-component mixture as reactants is connected to the reactant pipeline. Optionally, a storage container for storing the aqueous multi-component mixture is connected to the reactant pipeline. A pump, for example, a high-pressure pump for compressing the aqueous multi-component mixture is connected to the reactant pipeline; optionally, a pump for a precipitant; optionally, a pump for circulating water; the precipitant pump is connected to a precipitant pipeline 14. If necessary, a processing plant will also be needed to cool and separate the gasification products into water and syngas. A water treatment plant may also be provided if necessary. A natural gas processing plant may also be built if required. Gas storage facilities, such as hydrogen, methane, syngas, low-pressure, medium-pressure, and high-pressure storage facilities, can be selected and connected to syngas pipeline 11.

[0131] The plant according to the invention can be used in various ways. Reactor 1 can also be integrated into an existing plant. Defective plants or individual defective modules of plants can be easily replaced.

[0132] Another object of the present invention is to provide a method for assembling a plant including a reactor 1 according to the present invention. Another object of the present invention is to provide a process for supercritical hydrothermal gasification carried out in many embodiments of the reactor 1 according to the present invention. One object of the present invention is to provide a process for supercritical hydrothermal gasification of an aqueous multicomponent mixture, comprising: introducing a compressed aqueous multicomponent mixture into the reactor 1 via a reactant conduit according to the present invention; heating heat exchangers WT1 9 and (if applicable) WT2 12 and (if applicable) WT3 13 in separation zone 3 of the reactor 1 according to the present invention to 550 degrees Celsius; separating recyclable material from the compressed aqueous multicomponent mixture into one to three valuable material components WF1, and (if applicable) WF2 and WF3, via separator A1, and (if applicable) separator A2 and (if applicable) separator A3; and heating heat exchanger WT4 in heating zone 4... 10. Heat to 600-750 degrees Celsius, preferably 610-720 degrees Celsius, and most preferably a maximum of 710 degrees Celsius; heat the heater in the second pressure space 16 to 600-750 degrees Celsius, preferably 610-720 degrees Celsius, and most preferably a maximum of 710 degrees Celsius; adjust the flow rate or quantity of supercritical water containing dissolved synthesis gas through the bypass valve, flowing through heat exchanger WT4 and the bypass; introduce compressed inert gas into the second pressure space 16. If necessary, discharge the compressed inert gas from the second pressure space 16. Remove the compressed water containing dissolved synthesis gas from reactor 1. The above process steps can be carried out in different sequences or in parallel.

[0133] Aqueous multicomponent mixtures used as reactants in reactor 1 typically comprise several compounds, often a great many different compounds. In many cases, aqueous multicomponent mixtures comprise mixtures of solid and liquid substances. Mixtures consisting of organic compounds and inorganic components are preferably used as aqueous multicomponent mixtures. In many cases, the exact composition of the aqueous multicomponent mixture is unknown and / or varies from batch to batch. Aqueous multicomponent mixtures may contain inorganic components such as metals and heavy metals or metal ions, metal salts, metal oxides, heavy metal ions, heavy metal salts, heavy metal oxides, phosphorus, phosphorus oxides, phosphates, nitrogen, nitrogen oxides, and ammonium. In many cases, the total amount of inorganic matter and solids is less than 10⁻⁵% (by volume), typically about 2% (by volume) of the aqueous multicomponent mixture.

[0134] The aqueous multicomponent mixture that can be used as a reactant in reactor 1 is, for example, an organic multicomponent mixture, such as sludge, sewage sludge, biological waste, waste from biogas plants, aqueous organic waste, industrial waste, municipal waste, animal waste, agricultural waste, garden waste, animal meal, vegetable waste, fruit pomace, fly ash, sewage sludge fly ash, food industry waste, drilling mud, sludge, feces, wastewater such as industrial wastewater, plastics, paper, and paperboard. According to the invention, the aqueous multicomponent mixture used as a reactant in reactor 1 must be pumpable. If the solid content of the solid or aqueous multicomponent mixture is too high, appropriate pretreatment is required, preferably pulverization and dilution.

[0135] The gasification products of supercritical hydrothermal gasification include syngas dissolved in supercritical water. Preferably, the gasification products consist essentially of supercritical water with syngas dissolved in it. This syngas essentially comprises hydrogen, methane, and carbon dioxide. The composition of the syngas may vary depending on the reactants used, the embodiment of reactor 1 according to the invention, and the specific reaction conditions.

[0136] Applications of the reactor 1 and the apparatus according to the invention are also the subject of this invention. For example, the reactor 1 and the apparatus according to the invention are used to produce syngas, hydrogen, and methane from an aqueous multicomponent mixture. For example, the reactor 1 and the apparatus according to the invention are used to separate phosphates and ammonium from an aqueous multicomponent mixture. For example, the reactor 1 and the plant according to the invention are used to produce fertilizer from an aqueous multicomponent mixture. For example, the reactor 1 and the apparatus according to the invention are used to separate metal salts from an aqueous multicomponent mixture. For example, the reactor 1 and the apparatus according to the invention are used to separate solids from an aqueous multicomponent mixture. For example, the reactor 1 and the plant according to the invention are used to separate sand from an aqueous multicomponent mixture. For example, the reactor 1 and the plant according to the invention are used to separate metals from an aqueous multicomponent mixture. For example, the reactor 1 and the plant according to the invention are used to treat an aqueous multicomponent mixture. For example, the reactor 1 and the apparatus according to the invention are used for treating or purifying water. For example, the reactor 1 and the plant according to the invention are used in energy supply. For example, the reactor 1 and the apparatus according to the invention are used in energy storage. For example, the reactor 1 and the apparatus according to the invention are used in waste treatment, water treatment, and energy supply systems.

[0137]

[0138]

[0139] Figure 1 A longitudinal section of a reactor 1 according to the invention is shown, which has an inner shell 2, a separation zone 3, a heating zone 4 and a residence zone 5, wherein the separation zone 3, the heating zone 4 and the residence zone 5 are arranged in an upright columnar shape.

[0140] Figure 2 The diagram shows a longitudinal section of reactor 1 according to the invention, comprising an inner shell 2, a separation zone 3, a heating zone 4, and a residence zone 5, wherein the separation zone 3, heating zone 4, and residence zone 5 are arranged as upright columns, an outer shell 6, a base plate 7, a steel scaffold 8, heat exchangers WT1 9, WT4 10, WT2 12, and WT3 13, piping 14, a funnel-shaped transition 18 from the annular gap of the heating zone 4 to the annular gap of the residence zone 5, and flange connections 19.

[0141] Figure 3 A longitudinal section of the reactor 1 according to the present invention is shown, which includes an inner shell 2, an outer shell 6, a bottom plate 7, a synthesis gas pipeline 11, a first pressure space 15, a second pressure space 16, and a third pressure space 17.

[0142] Figure 4 The invention is shown Figure 3 The enlarged area of ​​reactor 1 includes an inner shell 2, an outer shell 6, a synthesis gas pipeline 11, a first pressure space 15, a second pressure space 16, and a third pressure space 17.

Claims

1. A reactor (1) for supercritical hydrothermal gasification of an aqueous multi-component mixture under oxygen-free conditions to 25 to 35 megapascal, comprising a pressurizable sealed inner shell (2) which can be sealed in a compact manner and which surrounds a first pressure space (15), a separation zone (3) in the inner shell (2), which comprises a heat exchanger WT1 (9) for heating the compressed aqueous multi-component mixture up to 550 degrees Celsius and a separator A1 for separating recoverable materials in the form of valuable material components WF1 from the compressed aqueous multi-component mixture, wherein the valuable material components WF1 are enriched in solid substances, metal salts, phosphates and ammonium, a heating zone (4) in the inner shell (2) for heating the compressed aqueous multi-component mixture to 600 to 700 degrees Celsius after separation of the recoverable materials, which heating zone (4) comprises a heat exchanger WT4 (10) and a synthesis gas duct (11) for counter-current heating of the compressed aqueous multi-component mixture with supercritical water without mixing of the phases, a residence zone (5) in the inner shell (2) for supercritical hydrothermal gasification of the compressed aqueous multi-component mixture after heating to 600 to 700 degrees Celsius, which residence zone (5) comprises the synthesis gas duct (11), wherein the separation zone (3), the heating zone (4) and the residence zone (5) are arranged in an upright column, wherein the separation zone (3) is arranged in a lower portion of the upright column, the separation zone (3) is adjacent to the heating zone (4), the heating zone (4) is adjacent to the residence zone (5) in an upper portion of the upright column, and an outer shell (6) surrounding the inner shell (2) and a second pressure space (16) between the inner shell (2) and the outer shell (6), wherein the synthesis gas duct (11) is located inside the heating zone (4) and inside the residence zone (5), the synthesis gas duct (11) starts inside the residence zone (5) and is located below an upper end of the residence zone (5), and the synthesis gas duct (11) is open with respect to the upper end of the residence zone (5) so that the generated synthesis gas dissolved in the supercritical water flows into the synthesis gas duct (11), the synthesis gas duct (11) forms an annular gap with the inner shell (2) in a portion of the heating zone (4) or in the entire heating zone (4), wherein the synthesis gas duct (11) opens into and is connected to the heat exchanger WT4 (10), wherein the synthesis gas duct (11) leads from the heat exchanger WT4 (10) through the heat exchanger WT1 (9) for heating the compressed aqueous multi-component mixture to 550 degrees Celsius, wherein one or more heating elements are arranged in the second pressure space (16) in the area around the annular gap of the heating zone (4) for heating the compressed aqueous multi-component mixture in the heating zone (4) to 600 to 700 degrees Celsius.

2. Reactor (1) according to claim 1, wherein the annular gap of the heating zone (4) for heating the compressed aqueous multi-component mixture to the temperature for supercritical hydrothermal gasification is at least in the diameter of the partial area of the heating zone (4) almost equal to the diameter of the inner shell (2) in the partial area, so that there is still an annular gap between the synthesis gas duct (11) and the inner shell (2) for the compressed aqueous multi-component mixture to flow through the annular gap.

3. The reactor (1) according to claim 1 or 2, comprising a heat exchanger WT2 (12) in the separation zone (3) for heating the compressed aqueous multi-component mixture to 300 to 400 degrees Celsius; a separator A2 for separating a valuable material component WF2; a heat exchanger WT1 (9) for heating the compressed aqueous multi-component mixture to 400 to 550 degrees Celsius; and a separator A1 for separating a valuable material component WF1, wherein the valuable material component WF2 is enriched in solids and metal salts and the valuable material component WF1 is enriched in phosphates and ammonium.

4. The reactor (1) according to claim 3, comprising a heat exchanger WT3 (13) in the separation zone (3) for heating the compressed aqueous multi-component mixture to 200 to 300 degrees Celsius and a separator A3 for separating the valuable material component WF3; a heat exchanger WT2 (12) for heating the compressed aqueous multi-component mixture to 300 to 400 degrees Celsius; and a separator A2 for separating a valuable material component WF2; a heat exchanger WT1 (9) for heating the compressed aqueous multi-component mixture to 400 to 550 degrees Celsius; and a separator A1 for separating a valuable material component WF1, wherein the solids are enriched in the valuable material component WF3, the metal salts are enriched in the valuable material component WF2 and the phosphates and ammonium are enriched in the valuable material component WF1.

5. Reactor (1) according to claim 1 or 2, wherein the annular gap widens at the transition from the heating zone (4) to the residence zone (5) to reduce the flow rate of the compressed aqueous multi-component mixture.

6. Reactor (1) according to claim 1 or 2, comprising a heat exchanger WT4 (10) in the heating zone (4), a bypass and a bypass valve, the heat exchanger WT4 (10) and the bypass being arranged in the inner shell (2) and connected to the synthesis gas duct (11) and the heat exchanger WT1 (9), wherein the bypass bypasses the heat exchanger WT4 (10) and by means of the bypass valve the proportion of the gasification product flowing from the synthesis gas duct (11) through the heat exchanger WT4 (10) into the heat exchanger WT1 (9) and the proportion of the gasification product flowing from the synthesis gas duct (11) through the bypass into the heat exchanger WT1 (9) can be adjusted to adjust the heat transferred from the gasification product to the compressed aqueous multi-component mixture in the heating zone (4).

7. Reactor (1) according to claim 1, wherein the outer shell (6) can be closed in a pressure-tight manner and the second pressure space (16) comprises a compressible inert gas for matching the pressure in the second pressure space (16) to the pressure in the first pressure space (15), wherein the compressible inert gas comprises < 5 vol% hydrogen and at least 50 vol% nitrogen.

8. Reactor (1) according to claim 1, wherein the inner shell (2), the heat exchanger WT1 (9), the separator A1 and the walls of the synthesis gas duct (11) have a wall thickness of 5 mm or less.

9. Reactor (1) according to claim 4, comprising a heat exchanger WT4 (10) in the heating zone (4), a bypass and a bypass valve, the heat exchanger WT4 (10) and the bypass being arranged in the inner shell (2) and being connected to the synthesis gas duct (11) and the heat exchanger WT1 (9), the bypass bypassing the heat exchanger WT4 (10) and by means of the bypass valve the proportion of the gasification product flowing from the synthesis gas duct (11) through the heat exchanger WT4 (10) into the heat exchanger WT1 (9) and the proportion of the gasification product flowing from the synthesis gas duct (11) through the bypass into the heat exchanger WT1 (9) can be adjusted to adjust the amount of heat transferred from the gasification product to the compressed aqueous multi-component mixture compressed in the heating zone (4), and wherein the synthesis gas duct (11) is connected to the bypass and the heat exchanger WT4 (10), the bypass and the heat exchanger WT4 (10) are connected to the heat exchanger WT1 (9), the heat exchanger WT1 (9) is connected to the heat exchanger WT2 (12), the heat exchanger WT2 (12) is connected to the heat exchanger WT3 (13) for heating the compressed aqueous multi-component mixture in counterflow to the gasification product, wherein the heat exchanger WT1 (9), the heat exchanger WT2 (12), the heat exchanger WT3 (13) and the heat exchanger WT4 (10) are pillow-type heat exchangers designed to heat the compressed aqueous multi-component mixture uniformly and rapidly in the separation zone (3).

10. Reactor (1) according to claim 5, wherein the annular gap has the shape of a funnel at the transition from the heating zone (4) to the residence zone (5), the wide end of the funnel facing the residence zone (5).

11. Reactor (1) according to claim 4, wherein the separators Al, A2 and A3 are arranged one above the other in succession, the heat exchangers being rotated by 90 degrees relative to one another.

12. Reactor (1) according to claim 4, wherein the heat exchangers WT1 (9), WT2 (12) and WT3 (13) are pillow-type heat exchangers.

13. Reactor (1) according to claim 4, comprising a floor (7) which can be pressed tightly to the inner shell (2) and the outer shell (6), wherein the floor (7) comprises an opening for a line (14) for separating the valuable material component WF1, an opening for a line (14) for separating the valuable material component WF2 and an opening for a line (14) for separating the valuable material component WF3.

14. Reactor (1) according to claim 1, wherein the reactor comprises a floor (7) and the floor (7) is connected to the inner shell (2) and the outer shell (6) by means of flange connections.

15. Reactor (1) according to claim 1, wherein the inner shell (2) is made of thin metal sheets of a nickel-based alloy and has a wall thickness of 1.5 to 0.75 mm.

16. Reactor (1) according to claim 7, wherein the pressure difference between the first pressure space (15) and the second pressure space (16) is a maximum of + / - 5 bar.

17. Reactor (1) according to claim 1, wherein the second pressure space (16) comprises an inert gas and two layers of thermal insulation.

18. An apparatus comprising a reactor (1) according to claim 1, a product line and a reactant line connected to the first pressure space (15) of the reactor (1), a high pressure pump connected to the reactant line, a comminution apparatus and a dilution apparatus connected to the reactant line, and a gas line connected to the second pressure space (16) and a gas reservoir.

19. Use of a reactor (1) according to claim 1, a) for the production of hydrogen and methane from an aqueous multi-component mixture, and b) for the separation and, if necessary, recovery of valuable materials selected from the group consisting of phosphates, ammonium, metal salts, metals from an aqueous multi-component mixture, if necessary, c) for the production of fertilizers from an aqueous multi-component mixture, if necessary, d) for the treatment or purification of water.

20. Use according to claim 19, wherein the reactor (1) is used for the production of hydrogen and methane from an aqueous multi-component mixture, and 21. Use according to claim 19, wherein the reactor (1) is used for the separation and, if necessary, recovery of valuable materials selected from the group consisting of phosphates, ammonium, metal salts, metals from an aqueous multi-component mixture, if necessary.

22. Use according to claim 19, wherein the reactor (1) is used for the production of fertilizers from an aqueous multi-component mixture, if necessary.

23. Use according to claim 19, wherein the reactor (1) is used for the treatment or purification of water.

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