Process and device for producing methanol from biomass
Patent Information
- Application Number
- PCT/EP2026/060187
- Authority / Receiving Office
- WO · WO
- Patent Type
- Applications
- Current Assignee / Owner
- Priority Date
- 2025-04-15
- Filing Date
- 2026-04-08
- Publication Date
- 2026-10-22
Smart Images
Figure EP2026060187_22102026_PF_FP_ABST
Abstract
Description
[0001] Method and apparatus for the production of methanol from biomass
[0002] The invention relates to a process for the direct conversion of biomass via coal to water gas (water gas is a mixture of H2 and CO), which is subsequently converted to methanol (MeOH) using known methods. Coal is produced as an intermediate.
[0003] Concepts for using liquid methanol as a pressureless energy storage medium are known. The production of methanol from biomass (e.g., at 1000°C) is also known.
[0004] A disadvantage of this process is the large amount of tar produced, because coal is generated in excess as an intermediate step. Liquid bed reactors are frequently used, but fixed bed reactors or rotary kilns are also employed.
[0005] The object of the invention is to provide a simple process for producing methanol from biomass.
[0006] The yield should be good. It should contain as few contaminating byproducts as possible, such as nitrogen (N2), which are difficult and complicated to remove from gases. In particular, the water gas produced in the interim should be pure and have a suitably beneficial ratio of its constituents.
[0007] It should be possible to use biomass without prior, costly drying.
[0008] The problem is solved by the features of the independent claims. Preferred embodiments are described in the dependent claims.
[0009] The invention relates to a process for producing methanol from biomass, comprising the steps of:
[0010] 1. Continuous pressureless conversion of the biomass with hot steam (excluding air and oxygen) to water gas, comprising H2 and CO, in a reactor, by (the following steps 1a. to 1e.):
[0011] a. Continuous feeding of biomass and hot steam at a reactor inlet and contact of the biomass with the hot steam at this reactor inlet, whereby a reaction mixture is formed,
[0012] lb. Heating and contacting this reaction mixture with a catalyst in a heated reaction zone of the reactor, wherein the heating is carried out by means of an external heater located outside the reaction zone (i.e. outside the reactor),
[0013] lc. continuous or periodic separation of ash in a separator to form a mixture of synthesis gas with CO2 (the mixture can also be called product gas),
[0014] ld. Preheating of the steam used with this mixture of synthesis gas and CO2 in a heat exchanger,
[0015] le. (Continuous or periodic) removal of CO2 from this mixture (e.g.
[0016] in a gas scrubber) forming water gas, comprising H2 and CO, and 2. converting this water gas to methanol,
[0017] wherein the catalyst is a movable packing which is located on a lifting (i.e. upwards and downwards) movable or pivotable or rotatable plate with holes or slots.
[0018] The conversion of biomass to water gas in step 1 is complete.
[0019] The preferred ratio of H₂ to CO in the water gas is adjusted by controlling the ratio of biomass to water vapor in step 1a (continuous feed). Furthermore, it can be adjusted by the residence time (contact time) of the synthesis gas mixture in a post-reaction zone of the reactor after step 1b (and before or even only after step 1c) – the temperature there is preferably 200°C to <830°C. In this preferred case, this post-reaction zone would be located downstream of the reactor in the process direction. Preferably, a control unit for temperature regulation in this post-reaction zone is also provided.
[0020] Preferably, the water gas consists of the two components hydrogen and carbon monoxide (H2 and CO) and contains only unavoidable impurities in the range of a maximum of 15 vol.%, or even max. 10 vol.%, ideally max. 5 vol.%.
[0021] The "reactor" thus clearly comprises the reactor inlet and the reaction zone. The "reactor inlet" is located at the top of the reactor, allowing the biomass to fall downwards into the heated reaction zone by gravity. The "reactor inlet" is therefore located directly above the reaction zone, so that both feeds (a biomass feed and a steam feed) meet in this area, allowing the biomass to fall from the feed into the reaction zone below.
[0022] “Feeding” therefore means feeding into the reactor, where the reactor inlet is located directly in the upper area.
[0023] The sequence of areas or plant components, as also shown in sketch form in Fig. 1, in the direction of the material flow is thus (the corresponding process steps in brackets): reactor inlet with biomass feed and steam feed.
[0024]
[0025] (1a.) Reaction zone with catalyst and plate (1b.)
[0026]
[0027] Separator (1c.)
[0028]
[0029] Heat exchanger (1d.)
[0030]
[0031] Device for removing CO2 from the mixture (preferably a gas scrubber) (1e.)
[0032]
[0033] for conversion to methanol (2.).
[0034] A "separator" is a component used to remove solid materials, such as ash particles. Examples of suitable devices include cyclone separators and electrostatic precipitators.
[0035] The "ash" contains, for example, salts from the plants in the biomass, such as unreactive potassium carbonate or silica salts.
[0036] A "cyclone separator" is a component of a plant in which heavier particles, such as ash in this case, are forced outwards by the radial momentum of the gas flow and fall downwards due to their weight, with the gas flow being diverted upwards or to the side – in this case, the mixture of synthesis gas and CO2, as it is to be directed from step 1c. to the heat exchanger in step 1d. The gas flow is thus free of this ash.
[0037] In the invention, no air / O2 is added in steps 1a to 1e, only water vapor. Therefore, the product gas mixture explicitly contains no significant amounts of nitrogen, which is of great importance for the final conversion to methanol and, if necessary, for the recycling of unreacted product gases, and thus for the energy efficiency of the process. Small amounts of nitrogen can be released from the biomass during its gasification. Organic components of the biomass react in step 1b (and also in the separator in step 1c) to form gases, one of which is carbon dioxide (CO2). The gas mixture obtained (in addition to the CO2) is diffuse (i.e., not strictly defined) and is therefore called "synthesis gas".
[0038] “Synthesis gas and CO2” within the meaning of the invention thus means “reaction gas mixture obtained after step 1c. in the separator as well as CO2” or “product gas and CO2”.
[0039] The catalyst "plate," if rotatable, can be mounted symmetrically (i.e., with its axis of rotation in the center of the plate) or eccentrically (i.e., with its axis of rotation not in the center of the plate). The advantage of the plate is that any ash produced during the reaction can continuously fall through its holes or slots and be removed from the reaction zone, thus preventing it from adhering excessively to the catalyst during the subsequent reaction. If mounted symmetrically, it can be rotated around its axis of symmetry / rotation perpendicular to the plate surface. Ash can then be removed from the catalyst, for example, by pressure pulses or by lifting movements (e.g., defined (rhythmic) raising and lowering) of the plate. If mounted eccentrically, ash can be "shaken off" the catalyst simply by rotating around the axis of rotation, which is not symmetrically located in the center of the plate surface.With the "swivelable" version of the plate, the ash can be visibly removed from the catalyst by swiveling the plate.
[0040] In the "stroke-like moving" version, the plate can be moved up and down in a stroke-like and jerky manner.
[0041] The “catalyst” is preferably made of an inert material, such as pyrolite (cordierite; stable up to 1300°C) or rapox (Al2O3; stable up to 1700°C).
[0042] The holes or slots in the plate should be clearly large enough that the catalyst cannot fall through them.
[0043] Both the plate and the catalyst bed are clearly located in the heated reaction zone of the reactor.
[0044] The advantage of "external heating" is that it enables efficient and oxygen-free process operation. Oxygen can be dispensed with during the conversion of the biomass used.
[0045] The "mixture" formed in step 1c. is also recognizably formed in step 1b., but is further refined in the separator, as it continues to react there. Depending on the reaction procedure, the mixture consists of unreacted water vapor and a synthesis gas, which is largely (i.e., >70 vol%) water gas (i.e., H₂ and CO) and C₂, preferably consisting of water gas and CO₂ in addition to water vapor, comprising >85 vol% or even >95 vol%, alongside small amounts of trace gases such as N₂.
[0046] The “water gas” also consists largely (that is, >70 vol%) of ingredients, in this case H2 and CO, especially preferably >85 vol%, or even >95 vol%.
[0047] The second step, the "conversion of water gas to methanol", also includes the fact that the conversion of water gas to methanol takes place in a different reactor, so that pipes lead from the point of continuous CO2 removal (in step 1e.) to this other reactor for the conversion in step 2.
[0048] The conversion of water gas to methanol in step 2 takes place in a known manner, under high pressure with a suitable catalyst required for this reaction and, for example, by means of purification through distillation or rectification.
[0049] Finally, the subject matter of the invention also includes a plant for the production of methanol from biomass, in particular also for carrying out the process according to the invention, comprising:
[0050] IA. a reactor (30) for pressureless process operation with feeds for biomass (1) and hot steam (2) at a reactor inlet,
[0051] IB. a heated reaction zone (20) of the reactor with external heating and a catalyst (40),
[0052] IC. a separator (60) for the continuous or periodic separation of ash, and for the formation of a mixture (3) of synthesis gas with CO2,
[0053] I D. a heat exchanger (70) for preheating the steam (2) used by means of the mixture (3) of synthesis gas and CO2,
[0054] IE. Device for the continuous removal of CO2 from the mixture (3) to form water gas (4), comprising H2 and CO,
[0055] wherein the catalyst (40) is a movable bulk material (e.g., consisting of spheres, cubes, or other shaped parts) located on a movable, pivotable, or rotatable plate (60) with holes or slots. It is evident that all embodiments for the individual process steps also apply to the system according to the invention and its components, and vice versa. This also applies to preferred embodiments, which are described further later in this document. The association between the respective process step and the system component is self-explanatory to those skilled in the art. For example, the components listed as 1A. relate to process step 1a., and vice versa.
[0056] It also includes the provision of conduits for the individual material flows or the interposition of further components. According to the "sequence of areas or plant components" described above, conduits may be present in between, for example, between the reactor (reference numeral 30 in Fig. 1) and the separator (reference numeral 60), and so on. However, between the reactor inlet and the reaction zone, there should clearly be no conduit with a cross-section smaller than that of the reactor, so that the biomass can fall downwards by gravity.
[0057] Since the process can operate without pressure in steps 1a. to 1e., preferably no pressure relief valve is present in components 1A. to 1E., or these parts of the system are designed for operation without pressure.
[0058] Advantages
[0059] The core of the invention is that the inventive process makes it possible to produce water gas from biomass and water vapor in a continuous process without obtaining and having to separate tar or coal as by-products.
[0060] Furthermore, it is advantageous to achieve an H2:CO ratio of essentially 2:1 (i.e., 1.8:1, 2 to 2.2:0, 8) in the resulting water gas formed in step 1e by continuously adding biomass and water vapor to the described reactor. These are volume parts.
[0061] This water gas obtained in the meantime advantageously contains no CO2 (carbon dioxide) and no interfering amounts (> 5%) of nitrogen (N2) after step 1e.
[0062] It is advantageous to measure the composition of the water gas after step 1e., for example, in a dedicated storage container where the water gas is held before being converted to MeOH (measurement by GC / GC-MS). Furthermore, in the separator according to the invention, a further reaction can advantageously take place even after the gas has passed through the heated reaction zone of the reactor, e.g., in a post-reaction zone, which is beneficial for achieving the desired ratio and purity in the water gas. An advantage of the invention is that the isolation of intermediately formed carbon, tar, and soot is avoided—particularly during the reaction that takes place in step 1b. The carbon formed in the interim is not retained in the reaction zone.Rather, the biomass, including intermediately formed carbon, can be completely converted to the desired gas mixture directly with the steam, and any ash produced can be removed downwards (into an ash collection container) through the plate according to the invention. The advantage of the catalyst as a movable bed, as well as of the (movable, pivotable, or rotatable) plate with holes or slots, is that it is possible to remove ash residue from the surface of the catalyst by means of mechanical movements or reverse pressure pulses (i.e., from below through the plate and the catalyst bed upwards) – thus preventing clogging and allowing the gases to flow through the catalyst bed.
[0063] The heat required for the reaction in step 1b is not obtained through combustion with oxygen, but rather the biomass is reacted with the water vapor in the absence of oxygen, and the heat is supplied externally (e.g., by means of an electric heater). Advantageously, this method can produce relatively pure water gas, which contains no components other than hydrogen (H2) and carbon monoxide (CO).
[0064] Furthermore, the process also works with moist raw materials, such as moist biomass in this case, which therefore does not need to be dried beforehand.
[0065] No backflow may occur at the biomass feed point; therefore, the reactor must be designed to be gas-tight at that point.
[0066] Another advantage of the invention is that no sulfur removal is necessary. In contrast, prior art requires such sulfur removal when using hard coal or lignite. Biomass contains fewer sulfur compounds.
[0067] Furthermore, any remaining traces of sulfur dioxide are also automatically removed during the CO2 removal process in step 1e. Preferred embodiments
[0068] The material being processed is preferably a bulk material consisting of spheres, cubes, or other shaped parts. The steps should ideally follow the sequence described. However, it is possible that additional steps, such as further purification stages, may be interposed.
[0069] For example, it makes sense to pass the gas mixture obtained in step 1b through a post-reaction zone of the reactor, where the water-gas equilibrium (i.e., the equilibrium between H2 and CO) is established.
[0070] In a preferred embodiment of the invention, steps 1a to 1e take place at a pressure of 100 mbar to <2 bar, particularly preferably at 500 mbar to 1.5 bar; in particular, they can also take place without pressure at atmospheric pressure. The advantage of this pressureless process for steps 1a to 1e is that, on the one hand, the materials used can be selected more freely and the wall thicknesses can be reduced, which, among other things, enables better heat transfer through the reactor wall and is therefore process-critical.
[0071] In a further preferred embodiment of the invention, the separator is a cyclone separator or an electrostatic separator, in particular it can be a cyclone separator.
[0072] In a preferred embodiment of the invention, the external heating in step 1b is an electric heating element.
[0073] Preferably, following step 1e, the water gas is cryogenically dried before being converted to MeOH. This also cryogenically removes any remaining CO2 and, if present, SO2.
[0074] In a preferred embodiment of the invention:
[0075] • the holes and slots of the plate have a maximum diameter of 4mm or
[0076] The edge length of the shortest edge of the slots must not exceed 4 mm, and
[0077] • the catalyst in the form of spheres or cubes must have a diameter or edge length at least 0.5 mm larger (than that of the holes or slots) so that the catalyst cannot fall through the holes or slots of the plate.
[0078] Clearly, "diameter" refers to holes or spheres, and "edge length" refers to slots or cubes. The holes or slots could each have an area of 0.1–3 cm². 2 have. 2.5 cm is also conceivable. 2 ±20% (or even with relative range limits of ±10% or even ±5%). It is particularly preferred if the catalyst has a diameter or edge length 0.5-2 mm larger than that of the holes or slots.
[0079] In a further preferred embodiment of the invention, the reactor, comprising the reactor inlet and the reaction zone located below it, is a vertically installable tubular reactor, and
[0080] The plate is round with a diameter that corresponds to the inner diameter of the tubular reactor, minus 2-10cm (preferably minus 2-8cm or minus 2-6cm).
[0081] In the case of the rotatable eccentric mounting of the plate, there is thus advantageously an edge area between the outer edge of the plate and the inner wall of the reactor for the eccentric rotational movement, so that the ash that forms in the meantime can be shaken off the catalyst.
[0082] “Vertical” means that the longitudinal direction of the tubular reactor is vertical, so that the biomass inside the tubular reactor can fall downwards along its longitudinal axis.
[0083] The tubular reactor can, for example, have an inner diameter of 10-100cm, preferably 10-50cm or even only 10-30cm.
[0084] In another preferred embodiment of the invention:
[0085] The biomass is fed in by means of a controllable screw conveyor (as part of the biomass feed system),
[0086] The hot steam is supplied by means of a controllable steam generator, and
[0087] To prevent condensation in the area of the screw conveyor, some of the obtained “mixture of synthesis gas with CO2” and / or water gas is added.
[0088] so that in the water gas, which is to be converted in step 2, a volume ratio of H2:CO of essentially 2:1 is established, that is, 1.8:1.2 to 2.2:0.8.
[0089] The ratio is best measured using GC / GC-MS after calibration. The values given therefore correspond to volume fractions. Regarding the last point: The "mixture of synthesis gas with CO2," which is intended to keep the screw conveyor dry, can be diverted either directly from the separator (after step 1c) or only after the heat exchanger (after step 1d) and fed to the screw conveyor.
[0090] Ideally, there is at least one control unit for controlling the screw conveyor, the steam, or both. This allows the target H2:CO ratio of 2:1 (by volume) to be set in the water gas.
[0091] It also corresponds to a preferred embodiment of the invention if, during the movable packing of the catalyst on the (stroke-like movable or pivotable or rotatable) plates during step 1b, reverse pressure pulses, i.e., pressure pulses passing from below through the catalyst to the top, are applied at regular intervals.
[0092] "At regular intervals" means, for example, pressure surges every 0.5 seconds to 10 minutes. Regular piston movement to generate such a pressure surge is also included.
[0093] In another embodiment, the removal of the ash is achieved by moving the plate. It can either be moved up and down in a jerky, reciprocating motion, or pivoted or rotated (around a symmetrically or eccentrically mounted axis of rotation). It is also possible to combine both embodiments (i.e., plate movement with pressure pulses).
[0094] In another preferred embodiment of the invention:
[0095] • The biomass is brought to a residual moisture content of 20-40 wt.% before being added in step 1a. and / or
[0096] • In step 1a. the continuously supplied starting materials (biomass and water vapor) together introduce a total amount of water of 0.517kg-1kg water per kg of dry biomass (especially preferably 0.3-0.4kg water (per kg of dry biomass).
[0097] “Total water” includes both the moisture content of the supplied biomass and the amount of supplied water vapor.
[0098] The aim here is to achieve a total water content of at least stoichiometric in relation to the carbon in the biomass to be converted to water gas. This results in a 2:1 (H₂ to CO₂) composition in the water gas. Particularly preferred in the three variants of this embodiment is the use of wood as the biomass.
[0099] In an advantageous embodiment of the invention, the biomass consists of wood, straw, leaves, bark pieces, grass clippings, aquatic plants, or mixtures thereof. Advantageously, these can be used in either a moist or dry state. It is particularly beneficial if the moisture content of the biomass mixture is determined using known methods before use and the mixture is then adjusted to the preferred residual moisture content (as described in the previous embodiment). This target residual moisture content of 20-40 wt.% is most easily achieved by selecting the appropriate mixture of biomass types, as these types naturally have very different moisture contents.
[0100] In the invention, it is further preferred if:
[0101] • in step 1b. the temperature of the reaction zone 800°C to 1700°C (preferably 800-1500°C, particularly preferably 800-1300°C, especially 900-1100°C), and
[0102] • the temperature in the separator is only 500-900°C.
[0103] It is particularly preferred if the areas are narrowed so that the temperature in the separator is a maximum of 200°C below the temperature of the catalyst (and the separator is particularly preferably a cyclone separator). Advantageously, the separator thus also has a high temperature, so that further reaction with any remaining water vapor can take place in the separator (post-reaction zone).
[0104] In another preferred embodiment, in step 1a., apart from the biomass and the hot steam, no other starting materials are introduced into the reactor inlet, except for any quantities of the water gas from step 1e. comprising H2 and CO (as described in another embodiment) that may be added there.
[0105] For the preferred variant with additional supply of water gas, a line for the return of the received water gas is visibly provided at the reactor.
[0106] In a further preferred embodiment of the invention, the continuous removal of CO2 in step 1e takes place using a countercurrent or cryogenic gas scrubber (particularly preferably countercurrent). Advantageously, this simultaneously results in the desalination of the resulting water gas. For example, the mixture (reference numeral 3) is contacted with K2CO3 or Na2COs or amines (each in liquid form, for example, as dilute solutions). In a further preferred embodiment, residual CO2 and, if applicable, SO2 are cryogenically removed, as already mentioned above.
[0107] It is also a preferred embodiment of the invention if
[0108] • the mixture of synthesis gas with CO2 has a temperature of <100°C after passing through the heat exchanger in step 1d, and / or
[0109] • the removal of CO2 in step 1e takes place at <100°C.
[0110] In another preferred embodiment, the catalyst is made of an inert material, selected from high-temperature ceramic (pyrolite (cordierite; stable up to 1300°C) or Rapox (Al2O3) or high-temperature steel.
[0111] In a further preferred embodiment of the invention, the biomass is wood with a composition determined after drying at 100°C for 24 hours of: 50 wt.% C, 43 wt.% O, 6 wt.% H, and 1 wt.% N, each within relative limits of ±20%. These are relative limits, not wt.%. Thus, 50 wt.% ±20% results in a range of 40 wt.% to 60 wt.%. Preferably, the relative limits are only ±10% or even just ±5%.
[0112] During the conversion of water gas to methanol:
[0113] - preferably, the water gas is fed to a high-pressure pump and compressed to a pressure of 150 to 450 bar,
[0114] - the compressed water gas flows through a second reactor (for conversion to methanol) with a catalyst and reacts at least partially to form methanol.
[0115] Preferably, at least a portion of the unreacted water gas from methanol formation (step 2 of the process according to the invention) is used:
[0116] • is recycled into the process after gas scrubbing (i.e., added to the water gas after step 1e.), and / or
[0117] Power is supplied to a generator for electricity generation, the generated electricity being used for the process, in particular for heating the reaction zone (20). (Byproducts such as methane are usefully removed here). Unless otherwise specified, it is advantageous to combine the different embodiments.
[0118] The invention will now be explained in more detail with reference to several preferred embodiments. These embodiments are not intended to limit the invention.
[0119] Fig. 1 shows the method according to the invention in outline form.
[0120] Fig. 2 shows the same sketch and indicates the locations of some of the process steps 1a to 1e according to the invention. Exemplary embodiments
[0121] Example 1:
[0122] In embodiment 1, wood is used as biomass, which has a composition (determined after drying) of:
[0123] 50 wt.% C, 43 wt.% O, 6 wt.% H and 1 wt.% N.
[0124] Assuming this composition, in this embodiment 0.517kg total water (this includes the residual moisture of the wood and the amount of water vapor) is used per 1kg of dry wood, i.e. 51.7 wt.%.
[0125] This corresponds to a residual moisture content of 34% by weight in the wood biomass, which is on average between moist wood from the forest and wood dried through storage (< 20% by weight).
[0126] 1 Biomass
[0127] 2 hot steam
[0128] 3 Mixture of synthesis gas with CO2
[0129] 4 Water gas, comprising H2 and CO
[0130] 5 MeOH (methanol)
[0131] 10 Reactor entrance
[0132] 20 heated reaction zones
[0133] 30 reactor
[0134] 40 catalyst
[0135] 50 plates with holes or slots
[0136] 60 separators (cyclone separators or electrostatic separators) 70 heat exchangers
Claims
Patent claims 1. Process for the production of methanol (5) from biomass (1), comprising the steps 1. Continuous pressureless conversion of the biomass (1) with hot steam (2) in the absence of air and oxygen to water gas (4), comprising H2 and CO, in a reactor (30), by a. Continuous supply of biomass (1) and hot steam (2) at a reactor inlet (10) and contact of the biomass with the hot steam at this reactor inlet, whereby a reaction mixture is formed; b. Heating and contacting of this reaction mixture with a catalyst (40) in a heated reaction zone (20) of the reactor, wherein the heating is carried out by means of an external heater located outside the reaction zone and lc. continuous or periodic separation of ash in a separator (60) to form a mixture (3) of synthesis gas with CO2, ld. Preheating of the steam used (2) by means of this mixture (3) of synthesis gas with CO2 in a heat exchanger (70), le. Removal of the CO2 from this mixture (3) to form the water gas (4), comprising H2 and CO, and 2. Conversion of this water gas (4) to methanol (5), wherein the catalyst (40) is a movable bulk material which is located on a movable, pivotable or rotatable plate (60) with holes or slots.
2. The method according to claim 1, wherein the separator is a cyclone separator.
3. Method according to one of claims 1 or 2, wherein steps 1a. to 1.e. take place at a pressure of 100mbar to <2 bar.
4. Method according to any one of claims 1 to 3, wherein • the holes and slots of the plate have a maximum diameter of 4mm or an edge length of the shortest edge of a maximum of 4mm, and • the catalyst in the form of spheres or cubes must have a diameter or edge length that is at least 0.5mm larger, so that the catalyst cannot fall through the holes or slots of the plate.
5. Method according to any one of claims 1 to 4, wherein the reactor (30), comprising the reactor inlet (10) and the reaction zone (20) located below it, is a vertically installable tubular reactor, and The plate is round with a diameter that corresponds to the inner diameter of the tubular reactor, minus 2-10cm.
6. Method according to any one of claims 1 to 5, wherein o the biomass (1 ) is supplied by means of a controllable screw conveyor, o the hot steam (2) is supplied by means of a controllable steam generator, and o to prevent condensation in the area of the screw conveyor, some of the obtained mixture of synthetic ash with CO2 (3) and / or water gas (4) is added, so that in the water gas, which is to be converted in step 2, a volume ratio of H2:CO of essentially 2:1 can be established, that is, from 1.8:1.2 to 2.2:0.
8.
7. Method according to one of claims 1 to 6, wherein, during step 1b, in the movable packing on the movable, pivotable or rotatable plates, reverse pressure pulses are applied at regular intervals, i.e., pressure pulses passing from below through the catalyst (40) upwards.
8. Method according to any one of claims 1 to 7, wherein • the biomass is brought to a residual moisture content of 20-40 wt.% before being added in step 1a. and • In step 1a, the continuously supplied raw materials biomass and water vapor together introduce a total amount of water of 0.517kg-1kg water per kg of dry biomass.
9. Method according to any one of claims 1 to 8, wherein • in step 1b. the temperature of the reaction zone (20) is 800°C to 1700°C and • the temperature in the separator (60) is 500-900°C.
10. Method according to claim 9, wherein the separator is a cyclone separator and the temperature in the separator (60) is a maximum of 200°C below the temperature of the catalyst (40).
11. Method according to any one of claims 1 to 10, wherein in step 1a. no other starting materials besides biomass (1) and hot steam (2) are introduced into the reactor inlet, except for any quantities of the water gas (4) from step 1e., comprising H2 and CO, that may be added therein.
12. A method according to any one of claims 1 to 11, wherein the continuous removal of CO2 in step 1e. takes place by means of a countercurrent or cryogenic gas scrubber.
13. A method according to any one of claims 1 to 12, wherein • the mixture (3) of synthesis gas with CO2 has a temperature of <100°C after passing through the heat exchanger in step 1d., and / or • the removal of CO2 in step 1e takes place at <100°C.
14. Method according to any one of claims 1 to 13, wherein the biomass wood has a composition, determined after drying, of: 50 wt.% C, 43 wt.% O, 6 wt.% H and 1 wt.% N, each within relative range limits of ±20%.
15. Equipment for carrying out the method according to any one of claims 1 to 14, comprising IA. a reactor (30) for pressureless process operation with feeds for biomass (1) and hot steam (2) at a reactor inlet, IB. a heated reaction zone (20) of the reactor with external heating and a catalyst (40), IC. a separator (60) for the continuous or periodic separation of dust and for the formation of a mixture (3) of synthesis gas with CO2, I D. a heat exchanger (70) for preheating the steam (2) used by means of the mixture (3) of synthesis gas and CO2, IE. Device for the continuous removal of CO2 from the mixture (3) to form water gas (4), comprising H2 and CO, wherein the catalyst (40) is a movable bed which is located on a movable or pivotable or rotatable plate (60) with holes or slots.