The present invention relates to a process for producing biochar according to the preamble of claim l.The present invention also relates to a reactor for producing biochar from renewable material according to the preamble of claim 14. Extensive use of coal and other fossil fuels globally largely contributes to the greenhouse gas emissions. It is recognized that it is possible to reduce such gas emission from the exisiting coal power plants by replacing larger or smaller shares of fossil coal fuel with charcoal from renewable sources without major reconstructions of existing process or infrastructure. Also the steel industry may replace fossil carbon fuels with renewable charcoal and thereby reduce emissions of carbon dioxide and other greenhouse gases. Thus there is a large demand for renewable charcoal produced at low cost in a process demonstrating high efficiency and having good environmental performance. However, during production of charcoal from renewable sources a large amount of exhaust gas such as carbon monoxide and non-combusted hydrocarbons are generated. If the temperature is unfavourable also tar and particles are formed which disturbs the process. Solid charcoal may be obtained as product of pyrolysis of biomass carried out at temperature above 300 °C. Pyrolysis of biomass is a thermal decomposition occurring in the absence of oxygene. Biomass may be pyrolised in a solid fuel gasification reactor. There are three different kinds of prior art solid fuel gasification reactors, counter current gasification reactor, co current gasification reactors and cross current gasfication reactor, with reference to flow direction of fuel and gasification air. Typically solid fuel gasification reactors have a low gasification temperature which results in high heat content in the gas in combination with high tar content. Since there is a large demand for charcoal from renewable resources it is desirable to eliminate or circumevent one or more of the above-identified disadvantages.

An object of the present invention is to provide a process for producing charcoal from renewable resources which operates with a high gasification temperature, and results in exhaust gas with a low tar content. Another object of the present invention is to provide a energy efficient continuous slow pyrolysis process for producing charcoal from renewable resources.

These objects are realised with a process for producing biochar comprising the following steps: -supplying biomass material into a material chamber of a reactor - drying the biomass material by evaporating moisture from the biomass material -pyrolysing the biomass material to obtain biochar and pyrolysis gas -supplying gasification air and pyrolysis gas to a reaction chamber in the reactor

-combustion of gasification air and pyrolysis gas in the reaction chamber

-removing exhaust gas from the reaction chamber

-heating the biomass material by indirect heat from the exhaust gas. Advantageous embodiments are described in the dependent claims and the following description.

In particular the invention provides a simple process for producing charcoal from feedstock such as wood waste. The inventive process can use wet raw material without pre-drying, this is also beneficial for the resulting exhaust gas which has a high heat value and very low tar contents. The process for producing charcoal according to the invention is further advantageous in that the obtained charcoal product has a very good quality.

The process according to the invention is suitable for producing renewable charcoal from several types of feedstock of renewable material such as biofuels, biomass, plant material, wood, wood waste, wood chips and forest residues such as bark.

Another advantage is that the feedstock is fed by gravitation through the reactor, thus no further means are necessary for conveying the feedstoch through the reactor. This also permits that the size of particles of the feedstock can be widely varied.

Apart from the advantageous production of charcoal, the inventive process provides high gasification temperatures and low outlet temperature of the exhaust gas.The generated exhaust gas may be used for heat production and to operate gas engines for production of electricity. Furthermore the electrical power consumption for running the inventive process is low.

Another advantage is that the coal conversion may be optimized when steam generated in the drying and pyrolyzing phase penetrate the hot charcoal bed. Furthermore, the process provides that the gasification air in the reaction zone reaches temperatures above 1000 °C and generate a reaction zone with temperatures above 1200 °C. This is advantageous in that the exhaust gas has a low tar content. Moreover, the process provides that output temperatures of the exhaust may be less than 600 °C, this is a result of the efficient indirect heat transfer of sensible heat from the exhaust gas to the biomass material, the product gas and the preheating of gasification air.

A further aspect of the invention relates to a reactor suitable for producing charcoal from renewable resources which acheives the corresponding advantages as the process according to the invention. Further advantageous features of the invention are defined in the dependent claims. In this specification the product obtained by the herein described process is referred to as renewable charcoal, charcoal from renewable material or biochar, these terms are considered alike and are used interchangeably throughout the specification. Furthermore the terms feedstock, raw material, injection material or input material are considered alike and are used interchangeably throughout the specification.

The expression "sensible heat" means the heat transferred to a thermodynamic system which results in a temperature change in the system. Sensible heat only increases the thermic energy in a system.

The invention will now be described in more detail with reference to an exemplifying embodiment thereof and also with reference to the accompanying figures in which Fig. 1 illustrates a flow chart for the process according to the invention

Fig. 2 schematically illustrates a sectional view of an embodiment of a reactor for producing renewable charcoal from renewable resources according to the invention.

Fig. 3 schematically illustrates the reaction zone of the reactor in Fig.2 in operation.

Fig. 1 schematically illustrates a flow scheme for the process for producing biochar from renewable material in a reactor according to the present invention wherein biomass material 100 is supplied to a biomass material storage container 60. The biomass material is further conveyed to a material chamber 10 wherein the biomass material is dried by evaporating moisture in a drying phase 103 by indirect heat 115 transferred from exhaust gas 110. In the material chamber the biomass material 100 is further pyrolysed in a pyrolysis phase 104 by transferring indirect heat 115 from exhaust gas 110 to obtain biochar 105 and pyrolysis gas 106. The heated pyrolysis gas 106, approx. 700 °C, biochar 105 and steam 111 are supplied to a reaction chamber 30 which holds a reaction zone 20. The heated pyrolysis gas 106 and gasification air 108 are mixed the reaction zone 20. The gasification air 108 is preheated to approx. 900 °C by indirect heat 115 transferred from exhaust gas 110 prior to entering the reaction zone. Furthermore ambient air 109 is fed into the reaction zone 20 together with the pyrolysis gas, to improve the quality of the obtained biochar.

In the reaction zone 20, pyrolysis gas 106 and gasification air 108 are mixed and combusted and the obtained exhaust gas 110 is removed from the reaction zone 20 and sensible heat in the exhaust gas is indirectly transferred to the biomass material and the gasification air, such that that the exhaust gas of approx. 600 °C leaves the reaction chamber 30, and finally the biochar 105 and ash is removed from the reaction chamber 30. Biochar is removed from the reaction chamber 30 by a outlet feeder 72 which feeds the biochar to a charcoal output container 70.

The process for producing biochar from biomass material in the reactor according to the invention includes the following reactions: Vapor is released and heated steam is formed in th drying phase. In the pyrolysis phase dry biomass is pyroiised to obtain char coal and pyrolysis gas. The pyrolysis gas contains mainly volatile hydrocarbons. In the reaction zone, preheated gasification air is introduced into the reaction zone and fuel and pyrolysis gas are combusted, resulting in high temperature exhaust gas which is used for indirect heating of the biomass material in the drying and pyrolysis phase. A part of the charcoal is combusted. When the gas, steam and pyroiised gas, penetrate the hot bed of char coal the steam will react with the carbon. The reaction will generate hydrogen via the water gas shift reaction.

CO _g +H20 _g - C02 _g +H ₂ (Reaction 1) However this reaction occurs high up in the reactor.

The following reactions also play a substantial role in the later, warmer parts of the reactor

C _s +H ₂ 0 ~> H _2g + CO _g Δ131 Kj/mol (Reaction 2) This reaction occurs when the excess steam passes the hot charcoal in the lower parts of the reactor and increases the amount of carbon that leaves the reactor as gas. However the reaction is endotherm and cools the hot charcoal bed. To secure reaction temperature some minor amount of air might have to be introduced in the char coal bed. In the warmest part of the reactor a Boudouard reaction plays a role and affects the relative content of carbon monoxide and carbon dioxide.

C _s + C0 _2g <-» 2 CO _g (Reaction 3) At temperatures above 700 °C the formation of carbon monoxide becomes favorable over carbon dioxide which makes the pyrolysis gas react with the hot charcoal bed to produce a more carbon monoxide rich gas. The raw pyrolysis gas is likely low on carbon dioxide so it is unlikely that this happens to any major extent. Both reaction (1) and (3) are reversible and are influenced by temperature, residence time and partial pressure of carbon dioxide and steam. Depending on the conditions in the reactor, these reactions will influence the gas composition and the charcoal production. One reason for the low amount of carbon dioxide early in the drying phase is due to the reactor initially being filled with a large amount of wet woodchips with a charcoal bed at the bottom. As the reactor heats up, the humidity will evaporate before the pyrolysis process can begin which produce large amounts of steam and relatively small amounts of pyrolysis gas. This steam reacts with the hot charcoal bed in reaction (2) and forms water gas (mostly carbon monoxide and hydrogen). Some carbon dioxide and water is produced as more air is introduced into the gas stream in the cracking zone.

As more of the biomass material is dried and the temperature rises, the pyrolysis gas, becomes more dominant which reacts via reaction (1) in the pyrolysis process to produce more carbon dioxide and hydrogen higher up in the reactor. As the amount of product gas increases, the amount of ethylene and acetylene also increases as they form only during pyrolysis and not from water gas.

The energy content of the gas is quite low as an energy content of 4-6 MJ/Nm3 is to be expected when gasifying biomass with air or air/steam. This is due to the high moisture content of the fuel as it favors hydrogen over carbon monoxide in the syngas which has lower energy content.

Fig.2 schematically illustrates a reactor 1 according to the invention. For purpose av illustration no biomass material or charcoal bed is shown in this figure. The reactor according to the invention may be describes as a solid fuel gasification reactor and operates as two step indirect regenerative heat exchanger provided with a first step wherein biomass material is indirectly pyrolysed without added oxidants to obtain renewable charcoal and a second step wherein preheated gasification air is used for gasifying some of the biochar from the first step and also cleaning the exhaust gas from soot and tar, whereby very hot exhaust gas is produced that is used to indirectly preheat the gasification air and pyrolyse the biomass material in the first step. This allows the hot exhaust gas to drive both the pyrolysis process and the preheating of the gasification air. In particular, the process may be defined as a continuous slow pyrolysis process wherein the sensible heat in the exhaust gas from the reaction is indirectly transferred to the biomass material to achieve drying and pyrolysis of the material to obtain renewable charcoal in an highly energy efficient reactor. The inventive reactor 1 for producing biochar from biomass material comprises a reactor vessel 5 which defines a biomass flow path extending from an inlet 7 to the reactor vessel 5 through to an outlet 71 from the reactor vessel, in which thermal decomposition of the biomass material progresses as the biomass material passes through the reactor vessel thereby obtaining renewable charcoal 105 and exhaust gas 110. The sensible heat in the exhaust gas indirectly dries and pyrolysis the incoming biomass feedstock in the absence of oxygen to renewable charcoal or biochar. Heat 115 from the heated exhaust gas is also indirectly transferred to the gasification air supplied to the reactor. This results in that the exhaust gas leaves the reactor at a reduced temperature which is advantageous.

The reactor vessel 5 comprises a material chamber 10, a reaction chamber 30, a gasification air conduit 40 and an exhaust gas channel 50 . The reactor vessel 5 is also provided with a biomass storage container 60 and a renewable charcoal output container 70.

The reactor vessel 5 comprises an longitudinally extended hollow enclosure arranged preferably in a vertical direction or near vertical direction. The reactor vessel and in particular the reactor chamber may be constructed of very heat resistant material such as Crom-Alloys , AI03 and/or different ceramics for high temperatures and reducing conditions.

The reactor vessel has an upper part which houses the material chamber 10 and a lower part which houses the reaction chamber 30. The rector vessel is configured as cone shape cylinder stacked onto a cylindrical reaction chamber.

The reactor vessel and the material chamber is provided with an upper end 5.1 which is closed and provided with a biomass material inlet 7 to supply biomass material from a biomass storage container 60 connected to the reactor vessel.

The biomass storage container 60 is provided with closing devices 61,62 arranged above and below the biomass storage container 60 to avoid that steam 111 or pyrolysis gas 106 moves upwards in the material chamber and into and through the container 60. The upper end 5.1 of the reactor vessel is further provided with a passage 8 for the exhaust gas channel 50.

The upper part of the reactor vessel, the material chamber 10, is provided with an outer mantle 11. The outer mantle 11 illustrated in Fig. 2 is provided with a cross section with an area which increases in the downwards direction, such that the outer mantle 11 of the reactor vessel has a conical form. Preferably, the outer mantle 11 is configured with an essentially circular cross section, however, it is also possible to have an oval or or square shaped cross section. The lower part of the reactor vessel houses the reaction chamber 30 which holds the reaction zone 20 and the charcoal bed 25 when the slow pyrolysis process of biomass material is in operation in the reactor vessel. In the lower end 5.2 of the reactor vessel, a biochar output container 70 is arranged below the reaction chamber 30. The reaction chamber is made of high quality construction grade steel and insulated inside with high temperature ceramic insulation.

The reactor vessel 5 further comprises an exhaust gas channel 50 and a gasification air conduit 40 arranged inside the material chamber 10 of the reactor vessel. In the embodiment of the reactor vessel shown in Fig. 2, the gasification air conduit 40 is arranged along a longitudinal centre line (marked out above the reactor vessel in Fig. 2) of the reactor vessel 5, and the gasification air conduit 40 is arranged inside the exhaust gas channel 50 such that the exhaust gas channel 50 and the outer mantle 11 of the reactor vessel are concentrically arranged around the gasification air conduit 40.

It should be noted that other configurations of exhaust gas channel 50 and gasification air conduit 40 arranged inside a material chamber 10 of a reactor vessel are also possible. Depending on the size of the reactor, the reactor vessel and material chamber may comprise several exhaust gas channels and gasification conduits. The dimensions and quantity of the material chambers, exhaust gas channel and gasification air conduit are designed based on case specific parameters.

The exhaust gas channel 50 is configured inside the material chamber 10 and is longitudinally extended between an channel outlet 50.1 arranged in the upper end 5.1 of the reactor vessel 5 and an channel inlet 50.4 arranged in the reaction chamber 30, such that, in operation of the reactor the exhaust gas is conveyed vertically upwards from the reaction zone.

The exhaust gas channel 50 has a channel wall, herein also called first heat transfer surface 54, which is made of a material suitable for efficient heat transfer. The whole channel wall, from the channel inlet 50.4 to the channel outlet 50.1 , operates as a heat transfer surface. The temperature of the surface varies along the length of the channel wall throughout the process. The exhaust gas channel 50 has a main section 50.2 arranged in the material chamber. The main section 50.2 is preferable cylindrical and has a cross section which is essentially the same along the whole length of the material chamber. However, the cross section area of the main section 50.2 is substantially smaller than the cross section area of the outer mantle 11 of reactor vessel 5 as illustrated in Fig. 2. The dimension of cross section of the exhaust gas channel 50 must be however adapted such that sufficient gas flow can pass through the channel with a suitable flow rate.

Fig. 3 shows that the exhaust gas channel 50 is enlarged in the lower end and is provided with a conical section 50.3 and an channel inlet 50.4 having a rim 50.5. The conical section 50.3 has an increasing cross section area in the downward direction towards the channel inlet 50.4. The channel inlet 50.4 may be provided with a cylindrical section 50.6 as shown in Fig. 3.

The reaction chamber 30 is further provided with distribution means 55 configured as a disc which is arranged below a gasification air outlet 41 and essentially aligned with the rim 50.5 of the channel inlet 50.4. The distribution means 55 has a cross section area which is smaller than the cross section area of the channel inlet 50.4 such that a gap 55.1 is formed between the distribution means 55 and the rim 50.5. The pyrolysis gas and steam entrained in the biochar and coming from the material chamber passes the gap 55. 1 to enter the reaction zone 20.

The conical section 50.3 and the channel inlet 50.4 forms a space wherein the reaction zone takes place when the reactor is in operation. The reaction zone 20 is further limited by the distribution means 55 which avoids that gasification air is directed on to the charcoal bed. Instead the gasification air is directed towards the heated pyrolysis gas.

The enlarged lower end of the exhaust gas channel is advantageous in that large volume of high temperature exhaust gas 110 can be removed from the reactor bed 25 but still keep a low exhaust gas flow rate in the region such that turbulence in the reaction zone 20 can be avoided. Turbulence may create an undesirable drag of particles with the exhaust gas flow 110 which should be avoided. It is therefore necessary to avoid high flow rates and turbulence in the reaction zone and the exhaust gas channel. The layout of the reaction chamber 30, the lower end of the exhaust gas channel 50, the gasification air conduit 40 and the distribution means 55 are therefore particularly configured to achieve a slow, low turbulent, gas movement in the reaction chamber 30 and the reaction zone 20. Another advantage is that low flow rates improves heat transfer from the exhaust gas 110 to the biomass material 100.

The exhaust gas 110 formed in the reaction zone 20 reaches a temperature of at least 1100 °C. The exhaust gas is conveyed through the exhaust gas channel 50 between the inside of the exhaust gas channel wall, the first heat transfer surface 54, and the gasification air conduit wall herein also referred to as second heat transfer surface 44 whereby heat 115 is indirectly transferred from the exhaust gas 110 and supplied to the biomass material bed 15 in material chamber 10 and to the gasification air 108 inside the gasification air conduit 40. The exhaust gas 110 is thereby cooled and leaves the exhaust gas outlet 50.1 with a temperature of approx. 350-400 °C. In one embodiment the reactor vessel 5 is provided with a ventilator (not shown in the figures) arranged in the gasification air conduit 40 to ensure under-pressure in the reactor. In the embodiment of the reactor vessel shown in Fig. 2, the gasification air conduit 40 is configured as a pipe and arranged inside the exhaust gas channel 50. The gasification air conduit 40 is preferably made of a material suitable for efficient heat transfer. The gasification air conduit 40 is longitudinally extended between a gasification air conduit inlet 42 arranged in a passage 4 in the upper end 50.1 of the exhaust gas conduit 50 and a gasification air outlet 41 arranged in the reaction zone 20. In operation, gasification air 108 is conveyed through the gasification air conduit 40 vertically downwards directly into the reaction zone 20.

The gasification air outlet 41 is located in the reaction zone 20 a short distance above the distribution means 55. This is advantageous in that the reaction and the temperature increase does not take place inside the charcoal bed 25 or directly in connection to the charcoal bed. An increase in the gas volume in direct connection with the charcoal bed gives rise to turbulence which may carry particles or non- combusted coal particles with the exhaust gas, which is undesirable.

The gasification air conduit 40 is configured with a cross section area substantially smaller than the cross section area of the exhaust gas channel 50. The gasification air conduit functions as second heat transfer surface 44 for transferring heat 115 from exhaust gas 110 moving upwards on the outside of the gasificiation air conduit 40 to preheat gasification air 108 conveyed downwards to the reaction zone 20.

The gasification air 108 may be supplied by an fan 112 (as indicated in Fig. 1). The gasification air flow rate determines the exhaust gas flow rate. The gasification air flow rate also determines the heat power output.

The reactor vessel 5 comprises a material chamber 10 is arranged around the exhaust gas channel 50. The material chamber is limited by an inner circumference formed by the exhaust gas channel wall 51, and an outer circumference formed by the outer mantle 11 of the reactor vessel, such that the material chamber 10 is provided with an annular cross section. AS shown in Fig. 2 the outer mantle wall 11 is conically formed in the longitudinal direction and the exhaust gas channel 50 has a cross section which is the same along the whole length of the channel. Therefore, the distance between the gas channel wall 51 and the outer mantle 11, herein also defined as the width of the material chamber 10, increases in the downwards direction. This is advantagoues in that the biomass material 100 gradually flows downwards through the material chamber 10 by gravity from a material inlet 7 in an upper end 5.1 of the reactor vessel to a biochar output 71 in a lower end 5.2 of the reactor vessel. This is advantageous in that the material is moved down with no additional mechanical means. The material chamber 10 is arranged to receive biomass material from a biomass supply container 60 connected to the upper end of the reactor vessel. In operation, the process according to the invention is suitable to utilise biomass material having a moisture content of more than 20 % and preferably less than 50%. The biomass material 100 forms a biomass material bed 15 inside the material chamber 10. The material bed 15 bears against the outer mantle wall 11 and the outside of the exhaust gas channel wall 51. The exhaust gas channel wall functions as a first heat transfer surface 54.

The layout of the reactor vessel creates benficial flow directions of the biomass material 100, the exhaust gas 110 and the gasification air 108 which is efficiently utilised for heat exchange purposes. In operation of the reactor the biomass material 100 and the gasification air 108 are conveyed downwards in the same direction. Furthermore, the biomass material 100 and exhaust gas 110 are moved, conveyed, in opposite directions relative to each other. As a consequence also the gasification air 108 and exhaust gas 110 are conveyed in opposite direction. This is advantageous in that the outgoing exhaust gas is counter current heat exchanged against both the gasification air and the biomass material.

The process according to the invention is operated as a continuous process. The process for producing the renewable charcoal 105 according to the invention is initited by firing of fuel in the charcoal outlet 71 below the reaction chamber. Furthermore, in operation, in a steady state condition, the process is self-sustaining, thus only a minor part of the supplied biomass material is combusted and generate the necessary heat for sustaining the process.

In one embodiment of the process the reactor vessel 5 is pressurized above atmospheric pressure, which improves the charcoal production.

By pressurizing the reactor vessel the dimensions of the reactor vessel may be reduced. Furthermore the energy content in the exhaust gas increases. In one example the energy content at atmospheric pressure is 4 J/Nm3, and if the pressure is increased to 2 Bar, the energy content in the exhaust gas is 8 MJ/Nm3.

Another advantage is that the dew point temperature and exergy value rises for the remaining steam which has the benefit that the steam can be used as heating medium in a district heating system. Another advantage is that the energy content in the exhaust gas increases with decreasing steam content. In a continuous process the biomass moves down through the material chamber 10 and through the process phases taking place in different process zones.

In a continuous process the upper part 10.1 of the material chamber 10 may be referred to as a drying zone. In operation heat 115 is indirectly transferred from heated exhaust gas 110 to wet feedstock 100 located in the upper part 10.1 of the material chamber 10 such that the feedstock dries and moisture evaporates. The evaporated moisture forms steam 111 which is moved downwards through a pyroiysis zone and pyroiysis phase of the material 105 and the charcoal bed 25. The temperature variation in the material chamber 10 determines the location of the different process zones.

The reaction chamber 30 receives the pyrolised material from the material chamber 10 and a charcoal bed 25 is formed around the periphery of the reaction chamber 30 and below the exhaust gas channel inlet 50.4 and a reaction zone 20 is formed above the bed of hot charcoal 25.

In the reaction zone, several reactions play a role. Heated pyroiysis gas is mixed with the preheated gasification air resulting in oxidation and combustion which generates heat.

The pyroiysis gas 106 is indirectly heated by the exhaust gas 110 in the pyroiysis process to approximately 700 °C prior to supplying the pyroiysis gas to the reaction zone 20 and the gasification air 108 is indirectly preheated by the exhaust gas to approximately 900 °C, prior to entering the reaction zone. The gasification/carburation temperature is in the range of 1000°C - 1300 °C, preferably the reaction zone reaches a temperature of at least 1100 °C.

Since the exhaust gas 110 provides indirect heat 115 for drying and pyroiysis of the biomass material and preheats the gasificiation air, the exhaust gas 110 is cooled dowm during the upwards movement in the exhaust gas channel, and at the exhaust gas outlet, the exhaust gas temperature is approximately 350- 400 °C.

As a result of the high gasification temperature, benifical thermal cracking of the gaseous biomass tars can take place in the reaction zone 20 resulting in very low amount of tar in the exhaust gas 110, and a high heat value may be acheived. This is advantageous in that less fuel energy from the coal conversion process is used in the gasification process. The heated steam from the drying phase enhances the tar cracking process.

In the charcoal bed 25 below the reaction zone and in the periphery of the reaction chamber 30, coal conversion by reduction takes place. In operation, vapor evaporated from biomass material from the drying phase is brought through the hot charcoal bed during coal conversion, which may reduce the charcoal production. The reaction chamber 30 is further provided with an air intake 35 arranged in the side walls of the reaction chamber and next to the charcoal bed 25, to supply ambient air 109 to the charcoal bed. This ensures the quality of the renewable charcoal obtained in the process.

The reactor vessel further comprises a material output, a renewable charcoal outlet 71, provided in the lower part of the reactor vessel to remove the renewable charcoal. A biochar output container 70 is connected to the charcoal outlet 71. The charcoal outlet 71 is provided with a rotating outlet feeder 72, configured as an inclined rotating disc which rotates by means of a motor 73. The residence time for supplied biomass material in the reactor depends on the outlet feeding rate. The outlet feeding rate determines the mass flow rate of the material movement by gravity through the material chamber which allows for a continuous operation and which also makes it possible to use the exhaust gas in a combustion motor to produce electricity. The outlet feeding rate is stepless regulated, which results in that different biochar product qualities can obtained, torrified as well as charred biochar.

The quality of the biochar obtainable by the method according to the invention depends on the type of feedstock material and the outlet feeding rate. However, the biochar produced by the inventive process has proven to have high specific surface, high micro-porosity and large absorption capacity. Typically, the process yields approximately 30% biochar in relation to biomass material supplied to the reactor. The production of biochar and biocoal can also be increased by the use of additional substrates.

The reactor further includes means for controlling and regulating the process. These means includes temperature sensors, thermocouples, differential pressure transmitters and thermal mass flow controllers arranged in several different disctinct positions on the outside of the exhaust gas channel wall, the first heat transfer surface 54, the outer mantle 11, the reaction zone 20, the exhaust gas channel 50 and the biochar outlet 71.

In operation, the temperature of the first heat transfer surface 54 is carefully controlled in the drying phase and the pyrolysing phase respectively. The temperature varies along the length of the first heat transfer surface 54 throughout the process, which influences the production process. The reactor has very few movable parts except for the outlet feeder. This is advantageous in that less maintenance is necessary.

It will be understood that structural modifications are possible within the concept of invention. It should be understood that the different embodiments are freely combinable with each other. The invention is therefore not restricted to the iliustrated and described embodiment thereof, since changes and modifications are possible within the scope of the accompanying claims.