Method for physical and thermo-chemical treatment of biomass and treatment plant

Abstract

The invention relates to a method for the physical and thermochemical treatment of biomass (5), wherein the biomass (5) is reduced in its water content in a drying device (4) and additionally ammonia (NH3) is released from the biomass (5) during drying. Subsequently the dried biomass (5) is pyrolyzed in a pyrolysis reactor (2) and the pyrolysis gas is further conducted to a combustion device (3) and combusted there to flue gas, or combusted to flue gas in a combustion plant unit (17), which flue gas is introduced into a mixing device (9), respectively. In the mixing device (9) oxygen (O2) is metered into the flue gas and introduced as drying gas directly into the drying device (4). While the drying gas is conducted through the drying device (4), sulfur dioxide (SO2) and / or sulfur trioxide (SO3) contained in the drying gas chemically reacts with ammonia (NH3) to form ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4). Additionally, the invention relates to a treatment device (1) for the physical and thermochemical treatment of biomass (5).

Description

[0001] The present invention relates to a combined method for the physical and thermochemical treatment of biomass, in particular organic waste products, such as slurries from sewage treatment plants, biogas plants, slaughterhouses, agriculture and forestry, farms, food industry, paper industry, chemical industry. In addition, the present invention also relates to a treatment plant which can be used for the physical and thermochemical treatment of biomass.

[0002] DE 10 2008 028 241 A1 describes a plant for the thermochemical treatment of biomass into combustion gas. The plant described therein consists of a screw reactor and a further reactor. In the screw reactor the biomass is dried and pyrolyzed in the absence of air, wherein the pyrolysis coke, pyrolysis gas and water vapor produced therein are jointly introduced into the further reactor and fill the further reactor to form a pyrolysis coke bulk material. In the further reactor, partial oxidation is carried out by substoichiometric addition of a gasification agent, in particular air. Herein, at least partial cleavage of long-chain pitch molecules takes place. The residual mass is drawn off from the further reactor downward by means of an extraction device. In order to prevent the inlet for the gasification agent and / or the outlet for the combustion gas in the region of the reactor wall from becoming blocked, a plurality of inner cavity extensions extending at least partially in the direction of gravity are provided. The combustion gas produced is introduced via its own outlet into a gas filter and a gas cooler. The purified combustion gas flowing out of the outlet end of the gas cooler is then introduced into, for example, a gas turbine. The electrical energy produced in the gas turbine can be fed into the power supply network, wherein the heat likewise produced can also be used to heat the screw reactor described above.

[0003] DE 10 2010 049 339 A1 describes a plant and a method for drying a material in a centrifugal shaft dryer. The material to be dried is further conveyed in the direction of passage successively through the dryer into sections arranged in succession and separated by means of a movable partition wall. The drying air introduced can flow through the drying chamber through connection openings provided in the region of the partition wall, or can be introduced and also discharged again in each of the sections. For the drying, flue gas from an external combustion chamber can also be used directly. Herein, a conventional oil or gas burner can be used. However, a biomass burner for pellets can also be used, as described in DE 203 21670 U1.

[0004] The object of the present invention is to provide a method and a treatment plant for the physical and thermochemical treatment of biomass, by means of which method or treatment plant problematic substances can be reduced or avoided without the use of additional means and a higher energy efficiency can be achieved throughout the operation of the treatment plant.

[0005] This object is achieved by the method and the treatment plant according to the claims.

[0006] The method according to the application is provided for the physical or thermochemical treatment of biomass, in particular organic waste products in treatment plants. The organic waste products are preferably different slurries from sewage treatment plants, slaughterhouses, agriculture and forestry, farms, the food industry, the paper industry and the chemical industry. In order to carry out the method, the following steps are carried out:

[0007] - providing biomass to be treated,

[0008] - providing a drying device,

[0009] - providing at least one pyrolysis reactor,

[0010] - providing at least one combustion device,

[0011] - providing at least one mixing device,

[0012] - feeding the provided biomass to be treated into the drying device, wherein the moisture contained in the biomass is reduced and additionally ammonia (NH3) is released from the biomass in the drying process,

[0013] - outputting the biomass to be treated from the drying device,

[0014] - feeding the biomass to be treated into the pyrolysis reactor,

[0015] - pyrolyzing the biomass in the pyrolysis reactor and simultaneously thermally decomposing the biomass into pyrolysis coke and pyrolysis gas,

[0016] - discharging the pyrolysis coke from the pyrolysis reactor and conducting the pyrolysis gas out,

[0017] - conducting the pyrolysis gas conducted out of the pyrolysis reactor into the combustion device and combusting the pyrolysis gas to form flue gas,

[0018] - conducting the flue gas out of the combustion device and into the mixing device,

[0019] - metering oxygen (O2) and / or at least one oxygen (O2)-containing gas into the flue gas in the mixing device and forming a drying gas, which, among other things, contains sulfur dioxide (SO2) and / or sulfur trioxide (SO3) in a gaseous aggregate state, respectively,

[0020] - conducting the drying gas out of the mixing device and into the drying device,

[0021] - guiding the drying gas through the drying device, wherein sulfur dioxide (SO2) and / or sulfur trioxide (SO3) contained in the drying gas, among others, chemically react with ammonia (NH3) to form ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4).

[0022] It is advantageous in the method steps selected here that the flue gas directed from the combustion device is introduced as so-called drying gas into the drying device directly after the metered addition of a volume proportion of oxygen or oxygen-containing gas. The thermal energy contained in the flue gas is thus used in the drying device together with the corresponding sulfur oxides contained therein. The addition of at least one additional substance for binding the ammonia gas generated or released in the drying process in the drying device is thus avoided, so that the additional substance does not have to be separately treated or filtered before the dryer exhaust gas or dryer exhaust air is output to the environment. In addition, a continuous, compact treatment facility is thus created, in which no additional facility components for providing the drying gas, such as a central heating station or other, are required for the long-term operation of the combustion device. The method steps are preferably carried out in the order previously specified.

[0023] In addition, it is advantageous if the drying gas is brought to a temperature value in the mixing device from a temperature value range whose lower limit is 100°C, in particular 300°C, and whose upper limit is 700°C, in particular 500°C. The possibility is thus created that the flue gas is brought to the temperature value or temperature value range required for use in the drying device by metered addition of substantially cooled ambient air in order to be able to carry out the drying process normally.

[0024] Another advantageous mode of operation is characterized in that the drying gas is brought to an oxygen content in the mixing device by metered addition of oxygen (O2) and / or at least one oxygen-containing (O2) gas from an oxygen content value range whose lower limit is 6% by volume, in particular 15% by volume, and whose upper limit is 20% by volume, in particular 17% by volume. By fixing, in particular reducing, the oxygen content in the drying gas output from the mixing device, it is possible to achieve a drying atmosphere in the drying device that prevents the risk of fire and / or explosion. In the drying process, among others, dust particles are formed, in particular at not too high drying temperatures, which can cause a dust explosion. This can comply with legally prescribed values, since the drying temperature is at a critical level.

[0025] Advantageously, there is also the method variant in which further flue gas from a central heating station is introduced into the mixing device. Thereby, a greater amount of drying gas can be provided in the possible combination for drying the biomass in the drying device. A still better or higher degree of drying of the biomass can thereby be achieved in order to be able to carry out a rapid treatment in the pyrolysis reactor subsequently. A still better energy efficiency can thereby be achieved.

[0026] Further, it is advantageous in the manner in which the further flue gas having a temperature value from the temperature value range whose lower limit is 100°C, in particular 200°C, and whose upper limit is 500°C, in particular 300°C, is introduced into the mixing device. Thereby, a predetermined temperature level of the drying gas can be achieved more simply in combination with the flue gas introduced from the combustion device, at least from the combustion of the pyrolysis gas.

[0027] Another advantageous mode of operation is characterized in that a sub-portion of the flue gas directed from the combustion device is tapped off before the introduction into the mixing device, this sub-portion of the flue gas is guided through a heat exchanger and the flue gas temperature is reduced, and the tapped-off flue gas is subsequently introduced into the combustion device for combustion. Thereby, an amount of thermal energy can be provided for an additional heating process. Furthermore, a further thermal energy can thereby be generated by guiding back to the combustion device and the combustion process.

[0028] The method variant in which ambient air is guided through the heat exchanger as the oxygen-containing gas (O2) and is raised in temperature by means of the flue gas guided through, and the ambient air is subsequently introduced into the mixing device and metered into the flue gas, is also advantageous. Thereby, the thermal energy contained in the tapped-off flue gas can be transferred to the tempering of the ambient air introduced into the mixing device. But in addition, a temperature control in the combustion chamber of the combustion device can thereby also be achieved by the flue gas guided back through the temperature reduction.

[0029] Another mode of operation is characterized in that the pyrolysis char discharged from the pyrolysis reactor is fed into a provided char treatment device and is further decomposed in the char treatment device into a solid, in particular pourable, residual product and a char off-gas. Thereby, a further additional treatment of the biomass already treated in the pyrolysis reactor can be carried out. A more intensive and more extensive treatment can thereby be achieved in a two-step process. A better recovery of materials contained therein, in particular phosphorus or phosphorus compounds, phosphates, potassium, calcium, magnesium, etc., can thereby be achieved depending on the selected biomass, for example organic waste products.

[0030] Further, it is advantageous if the residual products are discharged from the coke treatment device spatially separated from the coke offgas. Thereby additional gas can be provided for the combustion device, in order thereby to additionally increase the energy efficiency.

[0031] Another advantageous mode of operation is characterized in that the coke offgas, which is conducted from the coke treatment device, is introduced into the combustion device, and the coke offgas is combusted in the combustion device while forming flue gas and likewise is conducted from the combustion device. Thereby a still higher thermal energy can be provided in the combustion device.

[0032] It is also advantageous if the pyrolysis gas and the coke offgas are introduced into the combustion device separately from one another. By feeding the pyrolysis gas and the coke offgas separately from one another into the combustion device, a still more complete and better combustion can be achieved, whereby the thermal output can be additionally increased accordingly.

[0033] Another mode of operation is characterized in that the pyrolysis gas and the coke offgas are introduced into the combustion device jointly. Thereby a certain mixing can already be achieved before the two gases are introduced into the combustion device.

[0034] Another advantageous mode of operation is characterized in that ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4), which are formed in the drying device, are fed into the pyrolysis reactor jointly with the dried biomass. Thereby a subsequent joint treatment process can be carried out in the pyrolysis reactor.

[0035] The object of the present application, i.e. to provide a physical and thermochemical treatment process of biomass and at the same time to reduce or avoid problematic substances without using additional means and to achieve a higher energy efficiency during the entire treatment plant operation, is achieved independently and autonomously by another method according to the method steps given for the corresponding locations, if appropriate.

[0036] The other method is likewise provided for the physical or thermochemical treatment of biomass, in particular of organic waste products in a treatment plant. The organic waste products are preferably different slurries from sewage treatment plants, slaughterhouses, agriculture and forestry, breeding farms, the food industry, the paper industry and the chemical industry. In order to carry out the method, the following steps are carried out:

[0037] - providing biomass to be treated,

[0038] - providing a drying device,

[0039] - providing a combustion plant unit having at least one combustion reactor,

[0040] - providing at least one mixing device,

[0041] - feeding the provided biomass to be treated into the drying device, wherein the moisture contained in the biomass is reduced and additionally ammonia (NH3) is released from the biomass during drying,

[0042] - outputting the biomass to be treated from the drying device,

[0043] - feeding the biomass to be treated into the at least one combustion reactor,

[0044] - combusting the biomass in the at least one combustion reactor and simultaneously oxidatively converting the biomass into combustion products and flue gas,

[0045] - discharging the combustion products from the at least one combustion reactor and conducting the flue gas out,

[0046] - conducting the flue gas into the mixing device,

[0047] - metering oxygen (O2) and / or at least one oxygen (O2)-containing gas into the flue gas in the mixing device and forming a drying gas, which drying gas contains, among other things, sulfur dioxide (SO2) and / or sulfur trioxide (SO3) in a gaseous aggregate state, respectively,

[0048] - conducting the drying gas from the mixing device and into the drying device,

[0049] - guiding the drying gas through the drying device, wherein the sulfur dioxide (SO2) and / or sulfur trioxide (SO3) contained in the drying gas, among other things, chemically reacts with ammonia (NH3) to form ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4).

[0050] It is advantageous in the method steps selected here that the flue gas formed in the combustion plant unit and conducted from the combustion plant unit is introduced directly as a so-called drying gas into the drying apparatus after the metered addition of a volume proportion of oxygen or an oxygen-containing gas. The thermal energy contained in the flue gas is thus used in the drying apparatus together with the corresponding sulfur oxides contained therein. Hereby, the addition of at least one additional substance in the drying apparatus to bind the ammonia gas produced or released in the drying process is also avoided, so that the additional substance does not have to be separately treated or filtered before the dryer exhaust gas or dryer exhaust air is output to the environment. In addition, a continuous, compact treatment plant is also created, in which additional plant components for providing the drying gas, such as a central heating station or other combustion plants for long-term operation, are preferably not necessarily required. The method steps are preferably carried out in the order previously specified.

[0051] In addition, it is advantageous if the combustion plant unit is formed by a plurality of combustion reactors, and the flue gas formed in each case when combusting in the combustion reactors is fed to the mixing-in apparatus. The throughput can thus be increased overall in order to be able to combust a sufficiently large mass or quantity after the drying apparatus. This can be sufficient in a drying apparatus with a lower degree of drying.

[0052] Another advantageous mode of operation is characterized in that the drying gas is brought to a temperature value in the mixing-in apparatus from a temperature value range whose lower limit is 100°C, in particular 300°C, and whose upper limit is 700°C, in particular 500°C. The possibility is thus created that the flue gas is brought to the required temperature value or temperature value range for use in the drying apparatus by metered addition of substantially cooled ambient air in order to be able to carry out the drying process normally.

[0053] A method variant is also advantageous in which the drying gas is brought to an oxygen content in the mixing-in apparatus by metered addition of oxygen (O2) and / or at least one oxygen-containing (O2) gas from an oxygen content value range whose lower limit is 6% by volume, in particular 15% by volume, and whose upper limit is 20% by volume, in particular 17% by volume. By fixing, in particular reducing, the oxygen content in the drying gas output from the mixing-in apparatus, a drying atmosphere can be achieved in the drying apparatus which prevents the risk of fire and / or explosion. In the drying process, among other things, dust particles are formed, in particular at a not too high drying temperature, which can cause a dust explosion. This can comply with legally prescribed values, since the drying temperature is at a critical level.

[0054] A further mode of operation is characterized in that a sub-portion of the flue gas which is conducted from the combustion plant unit is tapped off before the introduction into the mixing device, this sub-portion of the flue gas is guided through a heat exchanger and the flue gas temperature is reduced, and subsequently the tapped-off flue gas is introduced into the combustion plant unit for the combustion. Thereby an amount of thermal energy can be provided for an additional heating process. Furthermore, it is then possible to generate additional thermal energy by guiding back into the combustion plant unit with its at least one combustion reactor and the combustion process.

[0055] Further, it is advantageous if ambient air is guided as the oxygen-containing gas (O2) through the heat exchanger and is temperature-increased by means of the guided-through flue gas, and subsequently the ambient air is introduced into the mixing device and metered into the flue gas. Thereby thermal energy contained in the tapped-off flue gas can be transferred to the tempering of the ambient air introduced into the mixing device. However, further thereby it is also possible to achieve a temperature control in the combustion chamber of the combustion plant unit by the guided-back flue gas by means of temperature reduction.

[0056] Finally, a further advantageous mode of operation is characterized in that ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4) formed in the drying device is / are fed together with the dried biomass into the combustion plant unit. It is then possible to carry out a subsequent joint treatment process in the combustion plant unit.

[0057] The object of the present application, namely to create a treatment plant for carrying out a physical and thermo-chemical treatment process of a biomass and at the same time to reduce or avoid problematic substances without using additional means and to achieve a higher energy efficiency during the entire treatment plant operation, is achieved independently and autonomously by the treatment plant according to the features given for the corresponding location, if appropriate.

[0058] The treatment plant is formed, inter alia, for carrying out the biomass treatment method and for carrying out the combustion thereof in a combustion plant unit. The treatment plant comprises

[0059] - a drying device which is formed for reducing the moisture contained in the biomass, and wherein further ammonia gas (NH3) can be released from the biomass during the drying process in the drying device,

[0060] - a combustion plant unit with at least one combustion reactor which is formed for combusting the biomass fed therein and at the same time for oxidatively converting the biomass into combustion products and flue gas,

[0061] at least one mixing-in device which is formed for metering in oxygen (O2) and / or at least one oxygen (O2)-containing gas into the flue gas which is conducted from the combustion plant unit into the mixing-in device in order to form a dry gas, wherein the dry gas formed by means of the mixing-in device contains sulfur dioxide (SO2) and / or sulfur trioxide (SO3) in a gaseous aggregate state, respectively, among other things,

[0062] a dry gas introduction line by means of which the at least one mixing-in device is in line connection with the drying device and which is formed for introducing the dry gas formed in the mixing-in device into the drying device.

[0063] An advantage achieved thereby is that the flue gas formed in the combustion plant unit and conducted from the combustion plant unit is directly introduced as so-called dry gas into the drying device after metering in a volume proportion of oxygen or oxygen-containing gas. The thermal energy contained in the flue gas is thus used in the drying device together with the respective sulfur oxides contained therein. Hereby, it is also avoided that at least one own additive substance is added in the drying device for binding the ammonia gas produced or released in the drying process, whereby the additive substance does not need to be separately treated or filtered before the dryer exhaust gas or dryer exhaust air is output to the environment. In addition, a continuous, compact treatment plant is thus also created, wherein preferably no additional plant components for providing the dry gas, such as a central heating station or other combustion plants for long-term operation, are necessarily required.

[0064] It can furthermore be advantageous if the combustion plant unit comprises a plurality of combustion reactors and each of the combustion reactors is in line connection with the mixing-in device. By using a plurality of combustion reactors, it is then also possible to feed or treat a larger amount of biomass in a shorter period of time than would otherwise be necessary.

[0065] A further embodiment is characterized in that the at least one combustion reactor is selected from a rotary tube furnace, a fluidized bed furnace, a furnace for dust ignition or Zykloidfeuerung, or a furnace with grate burners, such as a ladder furnace. A wide variety of biomasses can then be fed to its combustion device and the treatment plant can be adapted to the respective requirements.

[0066] A further possible embodiment has the following features: The treatment plant additionally comprises a central heating station and further flue gas from the central heating station can be introduced into the mixing-in device via an introduction line. It is thus possible to create the possibility that the mixing-in device can also be provided with further flue gas as required and that this is then introduced as mixed dry gas in the drying device.

[0067] For a better understanding of the present application, the application is described in more detail with the help of the following drawings.

[0068] In the drawings, largely simplified, schematic illustrations are shown:

[0069] Figure 1 First facility schematic of a treatment facility with the illustrated facility components;

[0070] Figure 2 Possible second facility schematic of a treatment facility with the illustrated facility components.

[0071] It is noted that in the differently described embodiments, identical parts are provided with identical reference signs or identical component numbers, wherein the disclosure contained in the entire description analogously can be transferred to the identical parts with identical reference signs or identical component numbers. Position information selected in the description, such as, for example, above, below, lateral, etc., refer to the directly described and illustrated drawings and are transferred to the new positions accordingly in the event of a change in position.

[0072] The term "in particular" is understood hereinafter in the sense that it can relate to a possible special form of embodiment or more detailed specification of an object or method step, but does not necessarily have to be the mandatory, preferred embodiment or the mandatory mode of operation thereof.

[0073] The terms "comprise", "have", "contain", "include", and any variations thereof, when used in this text, encompass a non-exclusive inclusion.

[0074] As an additional term, "optionally" can also be used. This is to be understood in the sense that this method step is essentially present, but can be used depending on the use conditions, but the method step is not necessarily mandatory.

[0075] In Figure 1 and Figure 2 In each case, a facility schematic is shown in which, by means of facility components that differ from one another, respectively, a flue gas can be formed, which is then used for drying the biomass to be treated. The difference lies only in those facility components for forming the flue gas. From the flue gas, a drying gas is then formed. The respective possible facility components and method steps will be explained in detail hereinafter.

[0076] A combined method for the physical and thermochemical treatment of biomass is proposed in each case. The term "thermochemical treatment" is understood to mean direct and indirect methods. In the direct method, combustion of the biomass takes place, wherein in the indirect method, pyrolysis or gasification of the biomass takes place.

[0077] At the outset, the possible process methods are briefly explained with respect to the difference in the oxygen fraction used therein and the combustion air ratio of the fuel-oxygen (air) mixture and the lambda value. The lambda value is a dimensionless characteristic number derived from the combustion theory, which gives the mass ratio of oxygen (air) to fuel in the ideal ratio according to the stoichiometric ratio for a theoretically complete combustion process. From this characteristic number, the combustion curve, the temperature, the production of harmful substances and the efficiency can be derived.

[0078] Pyrolysis is usually carried out at an oxygen fraction of 0% and thus at a lambda value of 0 (λ = 0 = ). However, in certain cases there can be a very small percentage of oxygen fraction even at pyrolysis.

[0079] Gasification is an intermediate state between pyrolysis and combustion. Gasification is usually characterized by a substoichiometric thermochemical oxidation reaction, thus forming a synthetic combustible gas with a lambda value greater than 0 but less than 1 (0 < λ < 1).

[0080] Depending on the material to be combusted, combustion requires a higher oxygen fraction, i.e. a lambda value of at least 1 or greater than 1 (λ > 1). However, in most cases or preferably, more oxygen (O2) is introduced or provided at combustion than is required or required for the oxidative reaction of the organic substances.

[0081] In Figure 1 a device diagram of a process plant 1 is shown in a simplified and very unrealistic manner, which comprises at least one pyrolysis reactor 2 for the biomass 5 to be processed, at least one combustion plant 3 and at least one drying plant 4.

[0082] The process plant 1 is essentially designed for the thermochemical treatment of the biomass 5 in a thermochemical process method or process. The treatment of the biomass 5 is carried out in a combined method, i.e. by means of physical treatment and thermochemical treatment. The so-called biomass 5 is understood here, inter alia, as organic waste products. The organic waste products include, inter alia, slurry or slurry-like substances from sewage treatment plants, slaughterhouses, farms, breeding farms, the food industry, the paper industry and the chemical industry. Sewage treatment slurry, slaughter waste, animal meal, excrement or many other substances can be involved here, for example. The term biomass 5 is understood as or implies all substances which contain or consist of organic compounds in a complex or less complex form. In order to be able to carry out the treatment of the biomass 5, the slurry must contain, for example, organic compounds which can be thermally reacted.

[0083] One possible aspect of the application can lie in the economic treatment of the biomass and the recovery of at least one material contained in the biomass 5. The material can be phosphorus (P) or phosphorus compounds such as P2O5, potassium, calcium, magnesium, etc., for example. Another possible aspect of the application can lie in the reduction or avoidance of problematic substances and energy consumption of the entire treatment plant 1.

[0084] Depending on the type and composition of the biomass 5, it is disposed of or further processed in a variety of ways beforehand. A first possibility is valorization by combustion in a waste incineration plant, a cement plant or similar. Another possibility, especially in the case of sewage treatment sludge, is to be sprayed onto fields in agriculture. However, here all the harmful substances, microplastics, etc. contained in the sewage treatment sludge at the same time are dispersed onto the fields and also into the groundwater. Finally, composting or soilization can also be carried out.

[0085] Before being fed into the drying device 4 and in turn into the pyrolysis reactor 2, at least a certain proportion of the quantity of biomass 5 to be treated, however especially the quantity of all the biomass 5 to be treated, can be dewatered in the dewatering device 6 to a humidity value from the following humidity value range, the lower limit of which is 70% by weight, especially 80% by weight, and the upper limit of which is 95% by weight, especially 90% by weight, relative to the total mass of the biomass 5.

[0086] Irrespective of or in addition to this dewatering step, at least a certain proportion of the quantity of biomass 5 to be treated, however especially the quantity of all the biomass 5 to be treated, is dried in the drying device 4 to a humidity value from the following humidity value range before being fed into the pyrolysis reactor 2, the lower limit of which is 3% by weight, especially 5% by weight, and the upper limit of which is 20% by weight, especially 10% by weight. However, it is preferred for the quantity of all the biomass 5 to be treated to be subjected to pre-drying. If a dewatering device 6 and a drying device 4 are provided, they can together form a drying plant.

[0087] The biomass 5 to be treated is preferably fed into the pyrolysis reactor 2 with or without the humidity reduction explained above. It is also possible here for the mass flow of the biomass 5 fed into the pyrolysis reactor 2 to be ascertained and stored or saved in the control device 7 if appropriate.

[0088] The control device 7 is also used to monitor the entire process of the biomass treatment from the delivery of the biomass until the end of the entire treatment process and to control all the plant parts or plant components in accordance with the pre-specified process steps. The respective communication connections between the control device 7 and the individual plant parts or plant components are shown in dashed lines. The biomass 5 can be fed into the pyrolysis reactor 2 by means of a gate system 8, for example a vertically rotating gate, preferably in a gas-tight manner.

[0089] If the pre-dried biomass 5 has been fed into the pyrolysis reactor 2, a thermo-chemical reaction or treatment of the biomass 5 takes place therein, which can be referred to as a pyrolysis process. Here, a thermal decomposition of the biomass 5 takes place into a pyrolysis coke and a pyrolysis gas, each having various constituent components. The pyrolysis coke is mostly formed as a solid fraction, which can also be referred to as a carbonization product.

[0090] The pyrolysis reactor 2 can be formed, for example, as a screw reactor, in which the thermal decomposition of the biomass 5 takes place at a temperature in the temperature range between 400°C, in particular 450°C, and 600°C, in particular 550°C. This process takes place under reduced oxygen conditions at a residence time of between 20 and 30 minutes. A lower oxygen concentration of less than 5% can be present in the pyrolysis reactor 2.

[0091] The pyrolysis gas produced is mostly an oil / gas mixture with a dust-like fraction in some cases. After the treatment of the biomass 5 in the pyrolysis reactor 2 is complete, the pyrolysis coke and the pyrolysis gas produced here are preferably discharged or guided out of the pyrolysis reactor 2 spatially separated from one another, as is shown in the present embodiment. It is also possible for them to be guided out of the pyrolysis reactor 2 together and separated later or subsequently.

[0092] The pyrolysis gas produced in the pyrolysis reactor 2 from the biomass 5 is itself guided into the combustion device 3, in which the pyrolysis gas is combusted, so that flue gas is formed. The flue gas produced or formed here is guided out of the combustion device 3 and into the own mixing device 9 located or arranged behind. The combustion product "flue gas" mostly still has a residual proportion of oxygen (O2), wherein the oxygen content in the flue gas can be about at most 5% by volume.

[0093] The mixing device 9 can comprise, among other things, a mixing chamber, in which at least one oxygen-containing gas, for example ambient air and / or oxygen (O2), is mixed in or metered in in addition to the flue gas from the combustion device 3. If at least the pyrolysis gas is combusted by means of the combustion device 3, thermal energy is produced. The flue gas guided out of the combustion device 3 has at least a temperature value from a temperature value range whose lower limit is 800°C, in particular 850°C, and whose upper limit is 1,200°C, in particular 1,000°C.

[0094] For the sake of clarity, the display of metering-in devices, valves, etc. is omitted. It is also noted that for control and / or monitoring, at or in the mixing device 9, a measuring assembly can be provided itself in order to know various parameters. Thus, for example, the temperature of all the gases fed into the mixing device 9 can be known separately. As further parameters, for example, the oxygen content and the proportion or content of the gases explained later can be known separately. The measuring assembly itself is in communication connection with the control device 7. For the sake of simplicity, only the connection line between the mixing device 9 and the control device 7 is displayed.

[0095] In the mixing device 9, on the one hand, ambient air and / or oxygen is metered into the flue gas, while, on the other hand, the temperature is reduced by at least one oxygen-containing gas and thus cooling takes place. The gas mixture leaving the mixing device 9 will be introduced directly and preferably without additional filtering processes into the drying device 4 and thus will be referred to as so-called drying gas in order to facilitate the differentiation of the gases present in the treatment plant 1.

[0096] The drying gas to be conducted from the mixing device 9 should have a temperature value from the temperature value range whose lower limit is 100°C, in particular 300°C, and whose upper limit is 700°C, in particular 500°C.

[0097] In addition, the drying gas to be conducted from the mixing device 9 should have an oxygen content from the oxygen content value range whose lower limit is 6% by volume, in particular 15% by volume, and whose upper limit is 20% by volume, in particular 17% by volume. The oxygen content should in particular preferably be not more than 17% by volume.

[0098] The drying gas to be conducted from the mixing device 9 contains, among other things, the gas sulfur dioxide (SO2). Sulfur dioxide is a colorless, mucous membrane-irritating, strongly smelling and sour-tasting toxic gas. The drying gas can additionally contain sulfur trioxide (SO3), which also has a gaseous aggregation state at the above-mentioned high temperatures.

[0099] In the following, another alternative treatment of the pyrolysis coke with possible method steps will be explained, which can be carried out, but does not necessarily have to be carried out or performed.

[0100] Now the pyrolysis char formed in the pyrolysis reactor 2 from the biomass 5 can be further conveyed into the char treatment device 10 for carrying out another additional treatment step. This treatment step can be carried out directly. However, it is also possible that the pyrolysis char, which is guided from the pyrolysis reactor 2, is conveyed to a temporary storage container 11 and temporarily stored there before being fed into the char treatment device 10. The pyrolysis char can be taken out from the temporary storage container 11 or further conveyed from the temporary storage container 11 to the char treatment device 10, for example by means of a conveying worm and a rotary feeder arranged behind the conveying worm.

[0101] It is to be noted that sulfur dioxide (SO2) and / or sulfur trioxide (SO3) can already be contained in the pyrolysis gas and / or in the char off-gas guided from the char treatment device 10 and / or also in the flue gas. The char off-gas generated in the char treatment device 10 can also be referred to as gasifier gas.

[0102] If the biomass 5, which is treated to pyrolysis char in the above-mentioned treatment step in the pyrolysis reactor 2, is located in the char treatment device 10, the pyrolysis char is further heat-treated in a possible subsequent treatment step. This treatment step can be carried out and forms another alternative way of further treatment. Here, the pyrolysis char is decomposed into a substantially solid residual product, in particular a pourable residual product, and a char off-gas. In this further heat-treatment in the char treatment device 10, gasification and / or also combustion can be carried out. The char treatment device 10 can also be referred to as a so-called oxidative char treater, which can enable or allow gasification and / or combustion. At least one material, which can be a target for recycling, is contained in the residual product, which is in most cases solid. The residual product is discharged from the char treatment device 10 spatially separated from the char off-gas, wherein the residual product can be collected in a not further specified container. The char off-gas can then itself be guided out of the char treatment device 10.

[0103] In the char treatment device 10, the pyrolysis char can be gasified from a temperature value from a temperature value range, the lower limit of which is 400°C, in particular 500°C, and the upper limit of which is 1,000°C, in particular 900°C.

[0104] It is also possible to guide the coke tail gas, which is conducted out of the coke treatment device 10, into the combustion device 3, wherein the coke tail gas is combusted in the combustion device 3, likewise forming flue gas. The flue gas, which is likewise produced or formed here, is conducted out of the combustion device 3. If both gases, i.e. the pyrolysis gas and the coke tail gas, are introduced into the combustion device 3, it is possible to introduce them into the combustion device 3 spatially separate from one another and to combust them in the combustion device. Irrespective of this, however, it is also possible to introduce both gases jointly into the combustion device 3, as is indicated by the dotted arrows. If both gases are combusted in the combustion device 3, flue gas, which was explained previously, is also formed from both gases and contains, inter alia, the gases sulfur dioxide (SO2) and / or sulfur trioxide (SO3).

[0105] For drying the biomass 5, in particular the slurry explained previously, a drying device 4 can be used, which is formed in various ways. For example, those explained in DE 10 2010 049 339 A1 can be used here. The drying gas used for this is formed in the process facility 1 of the subject matter here directly from the pyrolysis gas, which is combusted into flue gas in the combustion device 3, and, if appropriate, the coke tail gas, wherein in the mixing device 9 a volume proportion, which is predetermined in most cases previously, of oxygen has been metered into the flue gas and the drying gas is formed therefrom.

[0106] When the biomass 5 formed from organic waste products is dried in the drying device 4, the gas ammonia (NH3) is formed or released. Ammonia is a very strongly smelling, colourless, water-soluble and toxic gas at this temperature, which irritates the eyes and causes suffocation.

[0107] In the method step of the invention, at least these two gases are caused to chemically react by employing and using the drying gas, which contains, inter alia, the gas sulfur dioxide (SO2), and the ammonia (NH3). In this chemical reaction, a solid, crystalline substance is formed from the ammonia (NH3) and the sulfur dioxide (SO2), namely ammonium sulfite ((NH4)2SO3). It is also possible for the sulfur trioxide (SO3) to be contained in the drying gas at the same time.

[0108] It is thus possible for the reaction gases present to form ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4) with the ammonia (NH3). This depends on the temperature of the drying gas introduced into the drying device 4. The ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4) formed in the drying device 4 is fed together with the dried biomass 5 into the pyrolysis reactor 2 and subsequently pyrolyzed.

[0109] The gas leaving the drying apparatus 4 or being led out of the drying apparatus is referred to as dryer off-gas or dryer exhaust air. Due to the previously explained combination and conversion of ammonia gas (NH3), the dryer off-gas or dryer exhaust air is subjected to or requires certain chemical and / or physical cleaning again. Preferably, the dryer off-gas or dryer exhaust air is guided through a filter apparatus 13, which is shown schematically, before it is led out to the environment. Thereby, dust particles can be filtered out, which can have adhered to the dried biomass 5 in certain cases upon filter cleaning before being fed into the pyrolysis reactor 2.

[0110] It is also possible to introduce further flue gas from a central heating station (BHKW) 12 into the mixing apparatus 9. In order to achieve a cooling of the flue gas introduced into the mixing apparatus 9, the further flue gas should be introduced into the mixing apparatus 9 with a temperature value from a temperature value range, the lower limit of which is 100°C, in particular 200°C, and the upper limit of which is 500°C, in particular 300°C.

[0111] In order to increase the energy efficiency, it is also possible to propose that a sub- portion of the flue gas led out of the combustion apparatus 3 is tapped off before being introduced into the mixing apparatus 9. The tapped-off sub-portion can be referred to as a circulating gas and is subsequently guided through a heat exchanger 14 in order to output or reduce heat. The flue gas temperature of the circulating gas is thus reduced. The tapped-off flue gas is subsequently introduced into the combustion apparatus 3 in order to be combusted. The introduction into the combustion apparatus 3 can take place jointly with the pyrolysis gas and / or the coke tail gas or it is also possible to propose a separate introduction from one another, as shown. It is also shown that oxygen, in particular oxygen-containing ambient air, is introduced into the combustion apparatus 3 in order to combust the pyrolysis gas and / or the coke tail gas and, if appropriate, also the guided-back flue gas. Preferably, a self-contained introduction line is provided for each of the previously explained gases. The introduced ambient air can also be referred to as combustion air, which can be fed into the combustion apparatus 3 by means of the shown conveying apparatus 15.

[0112] If, as metered addition gas, for example, ambient air is selected as the oxygen- containing (O2) gas, the gas can be guided through the heat exchanger 14 before being introduced into the mixing apparatus 9 and the temperature of the gas is increased by means of the tapped-off sub-portion of the flue gas. Depending on the season, the ambient air has a local ambient temperature, from which the temperature is increased. After the ambient air stream metered into the gas flows through or past, the introduction into the mixing apparatus 9 takes place and the metered addition and mixing with the flue gas located in the mixing apparatus 9 takes place. Here, a self-contained conveying apparatus 15 with the same reference sign can also be provided, as shown. But it is also possible that only one conveying apparatus 15 is used to convey the ambient air to the heat exchanger 14 and to the combustion apparatus 3 with the corresponding laid-on line connections and valve assemblies.

[0113] At the beginning of the process of the biomass 5, this is first dried in the drying device 4 to a predetermined water content and thereby moisture, in particular water, is extracted. Since the pyrolysis reactor 2 is not yet in operation at this point in time, instead of drying gas, a flue gas formed from other fuels, such as natural gas, biogas, liquid gas, fuel oil, etc. and / or hot flue gases from other combustion processes, such as exhaust gases of combustion engines or alternative ignition devices, can be formed and fed into the mixing device 9 and there provide the drying gas for drying the biomass 5 in the drying device 4. The combustion engine can be, for example, a gas turbine and / or a gas engine. The alternative ignition device can be formed, for example, by a biomass boiler or the like. As soon as the dried biomass 5 can be fed into the pyrolysis reactor 2 and the pyrolysis reactor is in operation and the pyrolysis gas is conducted into the combustion device 3, the first supply of the drying device 4 can be provided.

[0114] With the previously explained processing plant 1, the provided biomass 5 can be subjected to a thermochemical treatment. At least the following method steps are carried out here:

[0115] providing a biomass 5 to be treated,

[0116] providing a drying device 4,

[0117] providing at least one pyrolysis reactor 2,

[0118] providing at least one combustion device 3,

[0119] providing at least one mixing device 9,

[0120] feeding the provided biomass 5 to be treated into the drying device 4, wherein the moisture contained in the biomass 5 is reduced and additionally ammonia (NH3) is released from the biomass 5 in the drying process,

[0121] outputting the biomass 5 to be treated from the drying device 4,

[0122] feeding the biomass 5 to be treated into the pyrolysis reactor 2,

[0123] pyrolyzing the biomass 5 in the pyrolysis reactor 2 and simultaneously thermally decomposing the biomass 5 into pyrolysis coke and pyrolysis gas,

[0124] discharging the pyrolysis coke from the pyrolysis reactor 2 and conducting the pyrolysis gas out,

[0125] conducting the pyrolysis gas conducted out of the pyrolysis reactor 2 into the combustion device 3 and combusting the pyrolysis gas to form a flue gas,

[0126] conducting the flue gas out of the combustion device 3 and into the mixing device 9,

[0127] - metering oxygen (O2) and / or at least one oxygen (O2) containing gas into the flue gas in a mixing device 9 and forming a dry gas, which comprises sulfur dioxide (SO2) and / or sulfur trioxide (SO3) in a gaseous aggregate state, respectively, among other things,

[0128] - conducting the dry gas from the mixing device 9 and introducing the dry gas into a drying device 4,

[0129] - guiding the dry gas through the drying device 4, wherein sulfur dioxide (SO2) and / or sulfur trioxide (SO3) contained in the dry gas, among other things, chemically react with ammonia (NH3) to form ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4).

[0130] In Figure 2 a further possible facility diagram of the individual embodiments of the treatment facility 1 is shown, which is likewise formed and arranged in such a way that it is able to carry out a physical and thermochemical treatment of a biomass 5, in particular organic waste products, such as sludge from sewage treatment facilities, slaughterhouses, farms, breeding farms, the food industry, the paper industry. Thus, here again the same reference numerals or component names as in the previously Figure 1 explained treatment facility 1 are used. In order to avoid unnecessary repetitions, reference is made to the detailed explanations in the previously Figure 1 explained treatment facility 1.

[0131] Unlike the previously explained treatment facility 1, the biomass 5 is combusted in the presence of oxygen, if desired, and the flue gas is provided or obtained at this time. The flue gas is introduced into the drying device 4, preferably and subsequently with the insertion of the mixing device 9 as required, for carrying out the drying process of the biomass 5.

[0132] The treatment facility 1 comprises, in terms of the facility, preferably a storage for receiving the biomass 5 to be treated, a dewatering device 6, if appropriate, and the drying device 4.

[0133] A conveying device 16 can be optionally but not mandatorily arranged after the drying device 4, by means of which the pre-dried or dried biomass 5 can be conveyed to a combustion facility unit 17 in a subsequent position, which comprises at least one first combustion reactor 18.

[0134] Depending on the quality or accumulation of the biomass 5 to be treated, the combustion facility unit 17 can also comprise a plurality of combustion reactors, wherein one further or second combustion reactor 19 is shown for the sake of clarity. The first combustion reactor 18 can be formed, for example, by a rotary tube furnace. The second combustion reactor 19 can be formed, for example, by a furnace with a grate burner, such as a ladder furnace or the like.

[0135] However, it is also possible that the combustion facility unit 17 comprises a plurality of combustion reactors 18, 19, which are respectively identically formed or which can use combustion reactors 18 or 19 based on the same working principle.

[0136] However, it is also possible that at least one of the combustion reactors 18, 19 or all of the combustion reactors 18, 19 are formed by a fluidized bed furnace working based on a fluidized bed ignition mode. However, it is also possible that at least one of the combustion reactors 18, 19 is formed for performing a dust ignition or a cyclone ignition.

[0137] The previously mentioned ignition systems are currently the most commonly used furnace types, by means of which a rotary tube ignition, a grate ignition, a fluidized bed ignition or also a dust ignition or a cyclone ignition can be performed. Any combination or multiple assembly of different furnace types can be set up as required. Thereby, different to be treated biomass 5 can be considered in terms of the process to be performed.

[0138] In this or these combustion reactors 18, 19, the to be treated biomass 5 is combusted with the supply of oxygen (O2) and / or at least an oxygen (O2) containing gas, wherein this combustion process can also be referred to as oxidation process. This likewise involves a physical and thermochemical treatment of the biomass 5, however by means of a combustion process.

[0139] In the pyrolysis process shown and explained previously in Figure 1 in the pyrolysis reactor 2, the biomass 5 is thermochemically converted or treated below stoichiometric ratio into pyrolysis coke and pyrolysis gas.

[0140] By means of the combustion process of the biomass 5 presented herein, the biomass is converted in the oxidation process with oxygen (O2) into combustion products and flue gas. The combustion products can be, for example, ash and / or can also be products still containing moisture. The combustion products are discharged or output from this or these combustion reactors 18, 19 and the flue gas is guided out in a respectively collected manner. Preferably, the flue gas can be guided out separately and independently of the combustion products, as respectively shown with one own line.

[0141] This or these flue gases are guided by means of a line into the mixing device 9, as already explained previously for the flue gas guided out of the combustion device 3.

[0142] In the mixing device 9, on the one hand, ambient air and / or oxygen is metered in to the flue gas which is introduced from the combustion plant unit 17, and, on the other hand, is reduced in temperature and thus cooled by at least one oxygen-containing gas. The gas mixture which leaves the mixing device 9 is subsequently introduced directly and preferably without additional filtering processes into the drying device 4 and is therefore referred to as the so-called drying gas in order to facilitate the differentiation of the gases present in the treatment plant 1. For this purpose, a not further designated drying gas introduction line can be provided.

[0143] The drying gas which is introduced from the mixing device 9 should have a temperature value from a temperature value range whose lower limit is 100°C, in particular 300°C, and whose upper limit is 700°C, in particular 500°C.

[0144] In addition, the drying gas which is introduced from the mixing device 9 should have an oxygen content from an oxygen content value range whose lower limit is 6% by volume, in particular 15% by volume, and whose upper limit is 20% by volume, in particular 17% by volume. The oxygen content should in particular preferably be no more than 17% by volume.

[0145] The drying gas which is introduced from the mixing device 9, among other things, contains the gas sulfur dioxide (SO2). Sulfur dioxide is a colorless, mucous membrane-irritating, strongly odoriferous and sour-tasting toxic gas. The drying gas can additionally also contain sulfur trioxide (SO3), which likewise has a gaseous aggregation state at the above-mentioned high temperatures.

[0146] In order to increase the energy efficiency, it can also be proposed that a sub-portion of the flue gas which is introduced from the combustion plant unit 17 is tapped off before the introduction into the mixing device 9. The tapped-off sub-portion can be referred to as a circulating gas and is subsequently guided through the heat exchanger 14 in order to output or reduce heat. The flue gas temperature of the circulating gas is thus reduced. The tapped-off flue gas is subsequently introduced again into at least one of the combustion plant units 17, in particular the combustion reactors 18, 19, in order to be further combusted.

[0147] It is additionally also shown that, in order to subsequently combust the guided-back flue gas, oxygen, in particular ambient air which contains oxygen, can also be introduced directly into at least one of the combustion plant units 17, in particular the combustion reactors 18, 19, and / or can be mixed into the circulating gas. It is also possible here for the oxygen (O2) and / or at least the gas which contains oxygen (O2) to be guided through a further heat exchanger which is not illustrated in more detail in order to be able to be warmed up.

[0148] Preferably, for each of the previously explained gases, a self-contained introduction line can be provided. The introduced ambient air can also be referred to as combustion air, which can be fed into at least one of the combustion plant units 17, in particular the combustion reactors 18, 19, at least by means of the illustrated conveying devices 15. Here, for each of the combustion reactors 18, 19, a self-contained conveying device 15 is provided.

[0149] If as metered addition gas, for example, ambient air is selected as the oxygen-containing gas (O2), the gas can be guided through a heat exchanger 14 before the introduction into the mixing device 9 and the temperature of the gas is increased by means of a tapped-off sub-portion of the flue gas. Depending on the season, ambient air has a local ambient temperature, from which the temperature is increased. After the ambient air flow, which forms the metered addition gas, flows through or past, the introduction into the mixing device 9 takes place and the metered addition and mixing of the flue gas located in the mixing device 9 takes place. Here, a self-contained conveying device 15 with the same reference sign can also be provided, as illustrated. However, it is also possible that only one conveying device 15 is used to convey the ambient air to the heat exchanger 14 and the combustion plant unit 17 with a correspondingly laid pipeline connection and valve assembly.

[0150] It is additionally possible that further flue gas from a central heating station (BHKW) 12 is also introduced into the mixing device 9 here. Again, a control device 7 can be provided in order to control or regulate the entire process plant 1 and the method flow and its plant components.

[0151] By means of the process plant 1 explained in Figure 2 the provided biomass 5 can be processed and subjected to the explained combustion process, among others. Here, at least the following method steps are carried out:

[0152] - providing biomass 5 to be processed,

[0153] - providing a drying device 4,

[0154] - providing a combustion plant unit 17 with at least one combustion reactor 18, 19,

[0155] - providing at least a mixing device 9,

[0156] - feeding the provided biomass 5 to be processed into the drying device 4, wherein the moisture contained in the biomass 5 is reduced and, in addition, ammonia (NH3) is released from the biomass 5 in the drying process,

[0157] - outputting the biomass 5 to be processed from the drying device 4,

[0158] - feeding the biomass 5 to be processed into the at least one combustion reactor 18, 19,

[0159] - combusting the biomass 5 in the at least one combustion reactor 18, 19 and simultaneously oxidizing the biomass 5 into combustion products and flue gas,

[0160] - discharging the combustion products from the at least one combustion reactor 18, 19 and conducting the flue gas out,

[0161] - conducting the flue gas into the mixing device 9,

[0162] - metering oxygen (O2) and / or at least one oxygen (O2) containing gas into the flue gas in the mixing device 9 and forming a dry gas, which comprises sulfur dioxide (SO2) and / or sulfur trioxide (SO3) in a gaseous aggregate state, respectively, among other things,

[0163] - conducting the dry gas from the mixing device 9 and into the drying device 4,

[0164] - guiding the dry gas through the drying device 4, wherein sulfur dioxide (SO2) and / or sulfur trioxide (SO3) contained in the dry gas, among other things, chemically react with ammonia (NH3) to form ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4).

[0165] In this treatment plant 1 the feeding and drying of the biomass 5 in the drying device 4 is also carried out, after which the dried biomass 5 is further conveyed and fed into at least one of the combustion reactors 18, 19. The oxidation and thus the oxidizing conversion of the biomass 5 into combustion products and flue gas takes place by the combustion process carried out in the combustion plant unit 17. When the combustion process is carried out with a lambda value greater than 1 (λ > 1), the flue gas formed or produced here also contains a proportion of oxygen (O2).

[0166] In contrast, in the case of the treatment plant 1 according to Figure 1 after the drying process is fed into the pyrolysis reactor 2 and is subjected to thermal treatment therein. As one of the decomposition products, a pyrolysis gas is formed here, which after being conducted out is conducted into the combustion device 3 and is combusted therein (jointly with the coke oven tail gas if appropriate) into flue gas.

[0167] The flue gas formed according to the method procedure according to Figure 1 or according to the method procedure according to Figure 2 is then conducted into the mixing device 9. The further method steps are carried out in the same way, respectively, and the dry gas formed in the mixing device 9 is conducted into the drying device 4.

[0168] The difference between the two method procedures explained previously lies only in the selection of the plant components for forming the flue gas from the biomass 5 to be treated.

[0169] It can also be proposed, however, that the processing plant 1 comprises a combination of the previously explained facility components for the thermochemical conversion or processing of the biomass 5. It is thus possible to use the pyrolysis reactor 2 (and, if appropriate, the coke treatment device 10) and the combustion device 3 and also the combustion facility unit 17 comprising at least one combustion reactor 18, 19 in parallel with one another. In both facility components, inter alia, a flue gas is formed from the biomass 5, which is then further introduced into the mixing device 9. It is thus possible to combine different thermochemical processing processes with one another depending on requirements.

[0170] With this chemical reaction or these chemical reactions, ammonia (NH3) is converted into a solid, mostly pourable aggregate state depending on the sulphur oxides contained in the drying gas. In other cases this can only be achieved with possible, additional, additionally added additive substances.

[0171] It is finally also mentioned that the individual method steps and their chronological order are not mandatorily carried out in the order given, but also a different chronological sequence can be implemented.

[0172] The examples show possible implementation variants, wherein it is noted at this point that the application is not restricted to the specifically shown implementation variants, but also different combinations of the individual implementation variants with one another are possible and the person skilled in the art is able to implement these variant possibilities with the application on the basis of the teaching regarding the technical processing.

[0173] The scope of protection is determined by the claims. However, the specification and drawings are intended to explain the claims. Individual features or feature combinations from the described different embodiments can be shown for independent application solutions. The underlying purpose of the independent application solutions can be gathered from the specification.

[0174] All information regarding numerical ranges in the present specification is to be understood as these numerical ranges simultaneously comprising any and all subranges thereof, for example a range of values from 1 to 10 is to be understood as comprising all subranges from the lower limit of 1 and the upper limit of 10, that is to say all subranges starting with a lower limit of 1 or more and ending with an upper limit of 10 or less, for example 1 to 1.7, or 3.2 to 8.1, or 5.5 to 10.

[0175] For the sake of clarity of sequence, it is finally noted that the elements are shown partially not to scale and / or enlarged and / or reduced for better understanding of the configuration.

[0176] List of reference signs

[0177] 1 processing plant

[0178] 2 pyrolysis reactor

[0179] 3 combustion plant

[0180] 4 drying plant

[0181] 5 biomass

[0182] 6 dewatering plant

[0183] 7 control plant

[0184] 8 lock system

[0185] 9 mixing plant

[0186] 10 coke handling plant

[0187] 11 temporary storage container

[0188] 12 central heating station

[0189] 13 filtering plant

[0190] 14 heat exchanger

[0191] 15 conveying plant

[0192] 16 conveying plant

[0193] 17 combustion facility unit

[0194] 18 first combustion reactor

[0195] 19 second combustion reactor

Claims

1. A method for the physical and thermochemical treatment of biomass (5), which is an organic waste product, wherein the following steps are carried out in a treatment plant (1): - providing biomass (5) to be treated, - providing a drying device (4), - providing at least one pyrolysis reactor (2), - providing at least one combustion device (3), - providing at least one mixing device (9), - feeding the provided biomass (5) to be treated into the drying device (4), wherein the moisture contained in the biomass (5) is reduced and additionally ammonia (NH3) is released from the biomass (5) in the drying process, - outputting the biomass (5) to be treated from the drying device (4), - feeding the biomass (5) to be treated into the pyrolysis reactor (2), - pyrolyzing the biomass (5) in the pyrolysis reactor (2) and simultaneously thermally decomposing the biomass (5) into pyrolysis coke and pyrolysis gas, - discharging the pyrolysis coke from the pyrolysis reactor (2) and conducting the pyrolysis gas out, - conducting the pyrolysis gas conducted out of the pyrolysis reactor (2) into the combustion device (3) and combusting the pyrolysis gas so that flue gas is formed, - conducting the flue gas out of the combustion device (3) and introducing the flue gas into the mixing device (9), - metering oxygen (O2) and / or at least one oxygen (O2)-containing gas into the flue gas in the mixing device (9) and forming a drying gas, which, among other things, contains sulfur dioxide (SO2) and / or sulfur trioxide (SO3) in a gaseous aggregate state, respectively, - conducting the drying gas out of the mixing device (9) and introducing the drying gas into the drying device (4), - guiding the drying gas through the drying device (4), wherein the sulfur dioxide (SO2) and / or sulfur trioxide (SO3) contained in the drying gas, among other things, chemically reacts with ammonia (NH3) to form ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4). The drying gas in the mixing device (9) is brought to a temperature value from a temperature value range, the lower limit of which is 100°C and the upper limit of which is 700°C. The lower limit of the temperature value range is 300°C. The upper limit of the temperature value range is 500°C. The drying gas in the mixing device (9) is brought to an oxygen content from an oxygen content value range, the lower limit of which is 6% by volume and the upper limit of which is 20% by volume, by metering in oxygen (O2) and / or at least one oxygen (O2)-containing gas. The lower limit of the oxygen content value range is 15% by volume. The upper limit of the oxygen content value range is 17% by volume. Further flue gas from a central heating station (12) is introduced into the mixing device (9). ​ ​ ​ ​ ​ ​ ​ ​ 2. The method of claim 1, wherein, ​ 3. The method of claim 2, wherein, ​ 4. The method of claim 2, wherein, ​ 5. The method according to claim 1 or 2, characterized in that, ​ 6. The method of claim 5, wherein, ​ 7. The method of claim 5, wherein, ​ 8. The method of claim 1, wherein, ​ 9. The method of claim 8, wherein, introducing the further flue gas having a temperature value from a temperature value range, the lower limit of which is 100°C and the upper limit of which is 500°C, into the mixing device (9).

10. The method of claim 9, wherein, the lower limit of the temperature value range is 200°C.

11. The method of claim 9, wherein, the upper limit of the temperature value range is 300°C.

12. The method of claim 1, wherein, splitting off a sub-portion of the flue gas led out of the combustion device (3) before the introduction into the mixing device (9), leading this sub-portion of the flue gas through a heat exchanger (14) and reducing the flue gas temperature, and subsequently leading the split-off flue gas into the combustion device (3) for combustion.

13. The method of claim 12, wherein, leading ambient air as the gas containing oxygen (O2) through the heat exchanger (14) and increasing the temperature by means of the flue gas led through, and subsequently leading the ambient air into the mixing device (9) and metering it into the flue gas.

14. The method of claim 1, wherein, pyrolysis coke discharged from the pyrolysis reactor (2) is fed into a coke treatment device (10) provided and further decomposed in the coke treatment device (10) into a solid, pourable residual product and a coke off-gas.

15. The method of claim 14, wherein, the residual product is discharged from the coke treatment device (10) spatially separated from the coke off-gas.

16. The method according to claim 14 or 15, characterized in that the coke off-gas led out of the coke treatment device (10) is introduced into the combustion device (3), and in the combustion device (3) the coke off-gas is combusted to form flue gas and likewise led out of the combustion device.

17. The method of claim 14, wherein, the pyrolysis gas and the coke off-gas are introduced into the combustion device (3) separately from one another.

18. The method of claim 14, wherein, the pyrolysis gas and the coke off-gas are introduced into the combustion device (3) together.

19. The method of claim 1, wherein, ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4) formed in the drying device (4) is fed together with the dried biomass (5) into the pyrolysis reactor (2).

20. A method for the physical and thermochemical treatment of biomass (5), which is an organic waste product, wherein the following steps are carried out in a treatment plant (1): - providing biomass (5) to be treated, - providing a drying device (4), - providing a combustion plant unit (17) having at least one combustion reactor (18, 19), - providing at least one mixing device (9), - feeding the provided biomass (5) to be treated into the drying device (4), wherein the moisture contained in the biomass (5) is reduced and additionally ammonia (NH3) is released from the biomass (5) in the drying process, - outputting the biomass (5) to be treated from the drying device (4), - feeding the biomass (5) to be treated into the at least one combustion reactor (18, 19), - combusting the biomass (5) in the at least one combustion reactor (18, 19) and simultaneously oxidatively converting the biomass (5) into combustion products and flue gas, - discharging the combustion products from the at least one combustion reactor (18, 19) and leading out the flue gas, - introducing the flue gas into the mixing device (9), - providing a mixing device (9) for mixing the flue gas with a further gas, - metering oxygen (O2) and / or at least one oxygen (O2)-containing gas into the flue gas in the mixing device (9) and forming a dry gas, which, inter alia, contains sulfur dioxide (SO2) and / or sulfur trioxide (SO3) in a gaseous aggregate state, respectively, - conducting the dry gas out of the mixing device (9) and into the drying device (4), - guiding the dry gas through the drying device (4), wherein sulfur dioxide (SO2) and / or sulfur trioxide (SO3) contained in the dry gas, inter alia, chemically react with ammonia (NH3) to form ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4).

21. The method of claim 20, wherein, The combustion plant unit (17) is formed by a plurality of combustion reactors (18, 19), and the flue gas formed in the combustion reactors, respectively, when combusting, is fed into the mixing device (9).

22. The method of claim 20 or 21, wherein, The dry gas is brought to a temperature value in the mixing device (9) from a temperature value range, the lower limit of which is 100°C and the upper limit of which is 700°C.

23. The method of claim 22, wherein, The lower limit of the temperature value range is 300°C.

24. The method of claim 22, wherein, The upper limit of the temperature value range is 500°C.

25. The method of claim 20, wherein, The dry gas is brought to an oxygen content in the mixing device (9) by metering oxygen (O2) and / or at least one oxygen (O2)-containing gas from an oxygen content value range, the lower limit of which is 6% by volume and the upper limit of which is 20% by volume.

26. The method of claim 25, wherein, The lower limit of the oxygen content value range is 15% by volume.

27. The method of claim 25, wherein, The upper limit of the oxygen content value range is 17% by volume.

28. The method of claim 20, wherein, A sub-portion of the flue gas conducted out of the combustion plant unit (17) is branched off before being introduced into the mixing device (9), this sub-portion of the flue gas is guided through a heat exchanger (14) and the flue gas temperature is reduced, and subsequently the branched-off flue gas is introduced into the combustion plant unit (17) for combustion.

29. The method of claim 28, wherein, Ambient air is guided through the heat exchanger (14) as the oxygen (O2)-containing gas and the temperature is increased by means of the guided flue gas, and subsequently the ambient air is introduced into the mixing device (9) and metered into the flue gas.

30. The method of claim 20, wherein, Ammonium sulfite ((NH4)2SO3) and / or ammonium sulfate ((NH4)2SO4) formed in the drying device (4) is fed into the combustion plant unit (17) together with the dried biomass (5).

31. A treatment plant (1) for the physical and thermo-chemical treatment of a biomass (5), which is an organic waste product, for carrying out the method according to any one of claims 20 to 30, the treatment plant (1) comprising - a drying device (4) formed for reducing the moisture contained in the biomass (5), and wherein, in addition, ammonia (NH3) can be released from the biomass (5) during the drying process in the drying device (4), - a mixing device (9) formed for metering oxygen (O2) and / or at least one oxygen (O2)-containing gas into the flue gas, and for forming a dry gas, which, inter alia, contains sulfur dioxide (SO2) and / or sulfur trioxide (SO3) in a gaseous aggregate state, respectively, - a combustion plant unit (17) having at least one combustion reactor (18, 19) formed for combusting and simultaneously oxidatively converting biomass (5) fed therein into combustion products and flue gas, - at least one mixing device (9) formed for metering oxygen (O2) and / or at least one oxygen (O2)-containing gas into flue gas led from the combustion plant unit (17) into the mixing device (9) in order to form a dry gas, wherein the dry gas formed by means of the mixing device (9) comprises sulfur dioxide (SO2) and / or sulfur trioxide (SO3), respectively, in a gaseous aggregate state, among other things, - a dry gas lead-in line, by means of which the at least one mixing device (9) is in line connection with the drying device (4), and which is formed for leading the dry gas formed in the mixing device (9) into the drying device (4).

32. A processing plant (1) according to claim 31, characterised in that The combustion plant unit (17) comprises a plurality of combustion reactors (18, 19) and each of these combustion reactors (18, 19) is in line connection with the mixing device (9).

33. A treatment plant (1) according to claim 31 or 32, characterised in that, The at least one combustion reactor (18, 19) is selected from a rotary tube furnace, a fluidized bed furnace, a furnace for carrying out dust ignition or swirl ignition, or a furnace with grate burners.

34. A processing plant (1) according to claim 31 or 32, characterised in that The treatment plant further comprises a central heating station (12), and further flue gas from the central heating station (12) can be led via a lead-in line into the mixing device (9).

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