METHOD AND SYSTEM FOR IMPROVING THE GREENHOUSE GAS EMISSION REDUCTION PERFORMANCE OF BIOGENIC FUELS, HEATING MEDIUMS AND COMBUSTION MATERIALS AND/OR FOR ENRICHING AGRICULTURAL AREAS WITH CARBON-CONTAINING HUMUS

Abstract

A method and a system for improving the GHG emission reduction performance of fuels, heating mediums and combustion materials and for enriching agricultural land with C-containing humus.

Claims

1. Method for converting biomass containing atmospheric carbon, preferably lignocellulose-containing biomass, more preferably straw, straw-containing input materials (e.g. solid manure) and/or wood, into GHG emission-reduced energy carriers, preferably biogas, bio-methane, pyrolysis gas, synthesis gas, bio-diesel, Fischer-Tropsch fuel, DME, bio-methanol or bio-ethanol, on the one hand, and chemically and physically stabilized atmospheric carbon, on the other hand, comprising the following steps: (1) Single-stage or multi-stage conversion of atmospheric carbon-containing biomass into another energy carrier, preferably a GHG emission-reduced energy carrier, more preferably by anaerobic bacterial fermentation into biogas or bio-methane, by alcoholic fermentation into bioethanol or ligno-ethanol, by gasification into pyrolysis gas, by carbonization into carbonization gas, by transesterification into bio-diesel, by Fischer-Tropsch synthesis into FT-fuel (FT-diesel, FT-gasoline, FT-kerosene, FT-methanol), by methanol synthesis into bio-methanol, by dimethyl ether synthesis into DME, (2) Generation of conditions that allow an at least partial chemical-physical stabilization of the atmospheric carbon still contained in the biomass conversion residues (e.g. digestion, fermentation, pyrolysis or synthesis residues), (3) Conduction of the at least partial chemical-physical stabilization of the atmospheric carbon still contained in the biomass conversion residues.

2. Method according to claim 1, in which the atmospheric carbon is at least partially stabilized in such a way that it is degraded (mineralized) within a given period of time to less than 30%, preferably less than 20%, in particular less than 10% and at best less than 5% by the processes of soil respiration, weathering, aerobic rotting and/or reaction with atmospheric oxygen, wherein the given period of time can be a selection from the following periods: 10 years, 30 years, 100 years, 500 years, 1,000 years, 10,000 years, 100,000 years, >100,000 years.

3. Method according to claim 1, in which the loss of atmospheric carbon or the loss of conversion residue dry substance which occur during the at least partial chemical-physical stabilization of the conversion residues is a maximum of 99%, preferably a maximum of 60%, more preferably a maximum of 40% and in particular a maximum of 30%.

4. Method according to claim 1, in which organic nutrients still contained in the residues of the single-stage or multi-stage biomass conversion are at least partially removed from these residues before the chemical-physical treatment, preferably together with process water, more preferably by a selection from the methods of centrifuging, decanting, pressing, separation, filtration, reverse osmosis, combination of these method steps, and in particular by recirculation of process water into the process, and/or in which the residues from the single-stage or multi-stage biomass conversion are pelletized or briquetted before the chemical-physical treatment, preferably after dewatering to >35% DS, in particular after dewatering to >50% DS and in particular after dewatering to >60% DS.

5. Method according to claim 1, in which the at least partial chemical-physical stabilization of the atmospheric carbon still contained in the residues of the single-stage or multi-stage biomass conversion is effected by a chemical-physical treatment of these residues, preferably by a thermal or thermo-chemical carbonization of these residues to form biochar/vegetable coal/biocoke, more preferably by a selection from the following thermo-chemical carbonization processes: pyrolysis, carbonization, torrefaction, hydrothermal carbonization (HTC), vapothermal carbonization, gasification and any combination of these treatment methods, and in particular by pyrolysis or torrefaction of dehydrated (dewatered) residues from the single-stage or multistage biomass conversion, wherein the dewatering preferably takes place to >35% dry substance (DS), more preferably >50% DS and in particular >60% DS.

6. Method according to claim 5, in which the dry mass loss which occurs during the carbonization of the conversion residues from the single-stage or multistage biomass conversion is a maximum of 99%, preferably a maximum of 60%, more preferably a maximum of 40% and in particular a maximum of 30% and/or in which the carbon content of the biochar/vegetable coal/biocoke produced is at least 20%, preferably at least 40%, more preferably at least 60%, in particular at least 70% and in the best case at least 80%, and/or in which the molar H/C ratio of the biochar/vegetable coal/biocoke produced is <0.8, preferably <0.6, and/or the molar O/C ratio of the biochar/vegetable coal/biocoke produced is <0.8, preferably <0.4.

7. Method according to claim 5, in which at least a portion of the biochar/vegetable coal/biocoke containing atmospheric carbon is sequestered (disposed of permanently) in an additional method step in the soil (geological formations), in stagnant waters, in aquifers or in the ocean, preferably in agricultural or forestry soils, more preferably in soils which are not or no longer used for agriculture or forestry, and in particular in bogs, desert or permafrost soils.

8. Method according to claim 5, in which the biochar/vegetable coal/biocoke containing atmospheric carbon is loaded (mixed) with nutrients prior to incorporation into soil formations, preferably with organic nutrients, more preferably with organic nutrients, which are contained in a selection of the following aqueous suspensions: slurry, percolate, swill, stillage from ethanol production, liquid residues from anaerobic fermentation, urine, seepage water from silages, (possibly treated or purified) process water, liquid fermentation mass, permeate, more liquid phase of dehydration, more solid phase of dehydration, any phase of separation, suspensions containing other nutrients and similar suspensions, and in particular with organic nutrients removed from the conversion residues to be carbonized before the carbonization of the conversion residues.

9. Method according to claim 5, in which the recuperated proportion of the conversion residues stream leaving the method step of the single-stage or multi-stage biomass conversion is divided into up to four partial streams before its carbonization in an additional method step, namely into the first partial stream “production of stabilized pyrolysis coal”, the second partial stream “production of partially stabilized torrefaction or HTC coal”, the third partial stream “production of unstabilized biochar/vegetable coal/biocoke” and the fourth partial stream “non-carbonized conversion residues”, wherein each of the partial streams can represent between 0% and 100% of the total stream (each partial stream can represent both the total stream and zero), wherein, in the method steps following the stream distribution, that is carried out with the respective partial stream which is indicated by the partial stream designation and/or wherein the first partial stream “production of stabilized pyrolysis coal” preferably has a proportion of >1% of the total stream, more preferably a proportion of >25%, in particular a proportion of >50% and in the best case a proportion of >75%.

10. Method according to claim 9, in which the up to four products which are produced in the method steps following the conversion residue distribution are produced in parallel or in series and/or in which they are mixed in any selection or combination to form a biochar/vegetable coal/biocoke mixture or to form a biochar/vegetable coal/biocoke conversion residue mixture, wherein the proportions of the up to four products can each be between 0% and 100% under the self-evident secondary condition that the sum of the proportions does not exceed 100%.

11. Method according to claim 5, in which the produced biochar/vegetable coal/biocoke, the biochar/vegetable coal/biocoke mixture or the biochar/vegetable coal/biocoke conversion residue mixture are produced at least in part from straw-containing conversion residues and/or in which the biochar/vegetable coal/biocoke, the biochar/vegetable coal/biocoke mixture or the biochar/vegetable coal/biocoke conversion residue mixture have a pH of >7.0, preferably a pH of >8.0, more preferably a pH of >9.0 and in particular a pH of >10.0, and wherein these basic products are preferably incorporated into acidic soils.

12. Method according to claim 1, in which chemically and physically stabilized atmospheric carbon, preferably atmospheric carbon carbonized at least partially into biochar/vegetable coal/biocoke, is incorporated into areas used for agriculture or forestry (arable soils, fields, forests, banks), preferably at least 5 t of biochar/vegetable coal/biocoke per hectare and 100 years, more preferably at least 50 t biochar/vegetable coal/biocoke per hectare and 100 years and in particular at least 100 t biochar/vegetable coal/biocoke per hectare and 100 years, and this C-application contributes to maintaining or increasing the humus content of the soil, preferably the C-containing humus content of the soil, more preferably the active nutrient humus content in the soil, in particular the passive permanent humus content in the soil, such that the proportion of biomass growth, preferably the proportion of straw growth, which had to remain in the fields prior to the application of the method for maintaining the humus content of the soil, can be reduced and thus increased access to the biomass growth, preferably to the straw growth, becomes possible, wherein the increased access based on the total biomass growth or the straw growth is preferably >0.1%-points, more preferably >30%-points, in particular >50%-points and in the best case >75%-points.

13. Method according to claim 1, in which atmospheric carbon dioxide (CO.sub.2) produced as a by-product, waste or residue is subjected to a selection of the following method steps: recuperation, purification, liquefaction, processing, sequestration (in geological formations, such as crude oil or natural gas reservoirs), substitution of fossil CO.sub.2, production of CO.sub.2-based energy carriers (syn-methane, syn-methanol), combination of these method steps.

14. Method according to claim 1, in which the energy carrier produced, which is preferably a selection of biogas, bio-methane, pyrolysis gas, synthesis gas, bio-diesel, bio-kerosene, Fischer-Tropsch fuel, bio-methanol, DME or bio-ethanol, is processed in such a way that it can be used as a fuel, heating medium or combustion material, preferably as a transport fuel, more preferably as a road fuel.

15. Method according to claim 1, in which, after the production, distribution and use of the energy carrier produced, which is preferably a fuel, more preferably a gas fuel and in particular bio-methane, there is a smaller amount of greenhouse gas in the atmosphere of the earth than after the production, distribution and use of an equal amount of energy of the fossil counterpart of the energy carrier produced, wherein mineral diesel fuel is the fossil counterpart for all diesel substitutes, mineral fuel for Otto engines (gasoline) the fossil counterpart for all substitutes of fuel for Otto engines, mineral kerosene the fossil counterpart for all kerosene substitutes, natural gas (CNG) the fossil counterpart for all natural gas substitutes, LNG the fossil counterpart for all LNG substitutes, LPG the fossil counterpart for all LPG substitutes and the weighted average of mineral fuel for Otto engines and mineral diesel the fossil counterpart for all other fuels, heating mediums and combustion materials.

16. Method according to claim 1, in which, after the production, distribution and use of the energy carrier produced there is a smaller amount of greenhouse gas in the atmosphere of the earth than before, i.e. the energy carrier produced is GHG-negative.

17. Method according to claim 1, in which the produced energy carrier (fuel, heating medium or combustion material) is mixed with a GHG-positive energy carrier (fuel, heating medium or combustion material), which is preferably a fossil counterpart of the produced energy carrier and more preferably a sustainable energy carrier, such that after the production, distribution and use of the produced energy carrier mixture there is a smaller amount of greenhouse gas in the atmosphere of the earth than after the production, distribution and use of an equal amount of energy of the fossil counterpart of the produced energy carrier, wherein mineral diesel fuel is the fossil counterpart for all diesel substitutes, mineral fuel for Otto engines (gasoline) the fossil counterpart for all substitutes of fuel for Otto engines, mineral kerosene the fossil counterpart for all kerosene substitutes, natural gas (CNGis the fossil counterpart for all natural gas substitutes, LNG is the fossil counterpart for all LNG substitutes, LPG is the fossil counterpart for all LPG substitutes and the weighted average of mineral fuel for Otto engines and mineral diesel the fossil counterpart for all other fuels, heating mediums and combustion materials.

18. Method according to claim 1, in which the generated energy carrier (fuel, heating medium or combustion material) is mixed with a GHG-positive energy carrier (fuel, heating medium or combustion material), which is preferably a fossil counterpart of the produced energy carrier and more preferably a sustainable energy carrier, such that after the production, distribution and use of the produced energy carrier mixture there is a smaller amount of greenhouse gas in the atmosphere of the earth than before, i.e. the energy carrier mixture is GHG-negative.

19. Method according to claim 17, in which mixing of the produced energy carrier is carried out with an energy carrier which is its fossil or its sustainable counterpart, wherein the mixing is preferably carried out in such a way that the resulting energy carrier mixture has a GHG emission value that is lower than the GHG emission value of the admixed energy carrier, and in particular in such a way that according to the life cycle analysis (WtW) or after stoichiometric analysis (TtW) the resulting energy carrier mixture has a GHG emission value which is less than/equal to 0.0 gCO.sub.2-eq/kWh.sub.Hi or less than/equal to 0.0 gCO.sub.2-eq/MJ.

20. Method according to claim 1, in which the physical-chemical stabilization of the atmospheric carbon takes place under oxygen deficiency and/or at reaction temperatures of 100° C.-1600° C., preferably at reaction temperatures of 200° C.-1,200° C., more preferably at reaction temperatures of 300° C.-1.000° C., in particular at reaction temperatures of 350° C.-1,000° C. and in the best case at reaction temperatures of 400° C.-900° C., and/or in which the heating of the residue to be treated from the single-stage or multi-stage biomass conversion to reaction temperature takes longer than 1 second, preferably longer than 10 minutes, more preferably longer than 50 minutes and in particular longer than 100 minutes.

21. Method according to claim 1, in which the method step of the single-stage or multi-stage conversion of biomass is preceded by the method step of selecting and/or harvesting or collecting at least one biogenic input material containing atmospheric carbon, wherein this input material is preferably characterized in that the selection is made from the input material groups of cultivated biomass, straw (cereal straw, corn straw, rice straw and the like; pure or as part of silage), farm manure, solid manure containing straw (solid cow manure, solid pig manure, poultry manure, dry chicken dung, horse manure, etc.), straw-containing residues from mushroom cultivation, slurry, swill, fresh grass-like plants (ryegrass, switch grass, miscanthus, giant reed and catch crops before and after main crops) and silages from these grass-like plants, whole-plant corn cuttings and corn silage, whole-plant cereal cuttings and silage from cereal whole plants, cereal and corn grains, wood, waste, residues from biomass processing, by-product from biomass processing, cellulose-containing non-food material, waste paper, bagasse, grape marc and wine lees, lignocellulose-containing biomass, residual forest wood, landscape conservation material, roadside greenery, cereals and other crops with a high starch content, sugar plants, oil plants, algae, biomass fraction of mixed municipal waste, household waste, biowaste, biowaste from private households, biomass fraction of industrial wastes including materials from wholesale and retail, agricultural and food industries as well as the fishing industry and aqua industry, slaughterhouse waste, sewage sludge, waste water from palm oil mills, empty palm fruit bundles, tall oil pitch, crude glycerine, glycerine, bagasse, molasses, grape marc, wine lees, stillage from ethanol production, nut shells, husks, cored corn cobs, biomass fractions of wastes and residues from forestry and forest-based industries (bark, twigs, pre-commercial thinnings, leaves, needles, tree tops, sawdust, wood shavings, black liquor, brown liquor, fiber sludges, lignin, tall oil), other cellulose-containing non-food material, other lignocellulose-containing material, bacteria, used cooking oil, animal fats, vegetable fats or combinations thereof.

22. Method according to claim 1, in which an additional step of recuperating at least a portion of the residues from the single-stage or multi-stage biomass conversion is performed between the step of single-stage or multi-stage conversion of the biomass and the step of the at least partial chemical-physical stabilization of the atmospheric carbon still contained in the residues of the biomass conversion.

23. Method according to claim 1, in which the method step of the single-stage or multi-stage conversion of the biomass into another energy carrier consists of an anaerobic bacterial fermentation, which is preferably carried out according to the solid fermentation process, more preferably the process of solid fermentation in garage fermenters or plug-flow fermenters, and/or in which before, during or after the method step of the single-stage or multi-stage conversion of the biomass this biomass is provided with at least one suitable admixture previously known from the relevant prior art, preferably an admixture from the selection: lime, enzymes, enzyme-containing solutions, fungi, acids, lyes, yeasts, water, recycled process water, purified process water, filtered process water, ultra-filtrated process water, process water subjected to reverse osmosis, treated process water, acid-water mixtures, lye-water mixtures, percolate, silage seepage juices, slurry, micro-organisms, any cereal grain stillage from ethanol production, any residue from the production of ligno-ethanol, any by-product/residue from the production of pyrolysis or synthesis gas, any by-product/residue from FT-synthesis, any by-product/residue from DME synthesis, any by-product/residue from methanol synthesis, any sugar beet stillage from ethanol production, combination of two or more of these additives.

24. Method according to claim 1, in which the biomass is subjected, before or after the method step of the single-stage or multi-stage conversion of the biomass into another energy carrier, to comminution, preferably chopping or shredding, more preferably the comminution combination consisting of chopping or shredding and grinding, and in particular the comminution combination consisting of bale disintegration, chopping/shredding and grinding and/or in which the comminution takes place in one or more stages to an average final particle length of <20 cm, preferably to an average final particle length of <5 cm, more preferably to an average final particle length of <10 mm, in particular to a final particle length of <3 mm and in the best case to a final particle length of <1 mm.

25. Method according to claim 1, in which the biomass is subjected, before, during or after the method step of the single-stage or multi-stage conversion of the biomass into another energy source, to a treatment which consists of a selection of the following treatment methods: comminution, soaking/mixing/mashing in cold water or aqueous suspensions including lyes and acids, soaking/mixing/mashing in 20° C.-100° C. warm water or aqueous suspensions including lyes and acids, biological treatment with fungi, pressurization to >1 bar-500 bar, treatment with >100° C. hot water, treatment with saturated steam, treatment by thermal pressure hydrolysis, treatment by wet oxidation, treatment by extrusion, ultrasonic treatment, steam reforming treatment, steam explosion treatment, drying, treatment with process water, treatment with process heat, treatment with enzymes, combination of a selection of these treatment methods.

26. Method according to claim 1, in which process heat from a method step is recycled into the process, preferably by means of heat exchange functioning in counterflow, and/or into a warming or heating step of the process, more preferably process heat from a thermal or thermo-chemical treatment before or after the single-stage or multi-stage conversion of the biomass into a warming or heating step, in particular process heat from the method step of the chemical-physical stabilization of the atmospheric carbon still contained in the conversion residues into a warming or heating step and at best process heat from the thermal or thermo-chemical carbonization of the conversion residues into a warming or heating step.

27. System for performing at the method of claim 1, comprising (a) devices for the single-stage or multi-stage conversion of biomass, preferably lignocellulose-containing biomass, more preferably straw-containing biomass, into a GHG emission-reduced energy carrier, (b) devices for generating conditions allowing an at least partial chemical-physical stabilization of the atmospheric carbon still contained in the residues of the single-stage or multi-stage biomass conversion (digestion, fermentation, pyrolysis or synthesis residues and the like).

28. System according to claim 27, in which the devices for the single-stage or multi-stage conversion of biomass consist of suitable devices previously known from the relevant prior art, preferably a selection of the following devices: devices for the anaerobic bacterial fermentation of biomass into biogas and/or bio-methane, devices for the alcoholic fermentation of biomass into bio-ethanol or ligno-ethanol, devices for the gasification of biomass into pyrolysis gas and/or pyrolysis slurry, devices for the carbonization of biomass into carbonization gas (weak gas), devices for the transesterification of vegetable oils into bio-diesel (FAME), devices for the hydration of vegetable oils in HVO (mineral oil refineries), devices for the refining of vegetable oils in HVO (NesteOil process), devices for the gasification/pyrolysis of biomass to process gas, devices for the conversion of biomass-derived process gas to synthesis gas, devices for the synthesis of biomass-derived synthesis gas to a Fischer-Tropsch fuel (FT-diesel, FT-gasoline, FT-kerosene, FT-methanol and the like), devices for the synthesis of methanol from biomass-derived gases, devices for DME synthesis, any combination of these devices.

29. System according to claim 27, in which the devices for generating conditions allowing at least partial chemical-physical stabilization of the atmospheric carbon still contained in the biomass conversion residues, include appropriate devices previously known from the relevant prior art, preferably devices for the chemical-physical treatment of these residues, more preferably devices for the thermal or thermo-chemical carbonization of these residues to biochar/vegetable coal/biocoke, in particular a selection from the following devices for the thermo-chemical carbonization of biomass to biochar/vegetable coal/biocoke: pyrolysis devices, carbonization devices, torrefaction devices, hydrothermal carbonization (HTC) devices, vapothermal carbonization devices, gasification devices, any combination of these devices, wherein the carbonization devices for the conversion residues are preferably suitable for carrying out the carbonization under oxygen deficiency and/or at reaction temperatures of 100° C.-1600° C., more preferably at reaction temperatures of 200° C.-1.200° C., in particular at reaction temperatures of 300° C.-1,000° C., in an even better case at reaction temperatures of 350° C.-950° C. and in the best case at reaction temperatures of 400° C.-900° C.

30. System according to claim 27, in which the devices for the at least partial chemical-physical stabilization of atmospheric carbon are suitable for carbonizing the residues from the single-stage or multi-stage biomass conversion to such biochar/vegetable coals, or to such biocoke that their proportion of atmospheric carbon is preferably degraded (mineralized) within a certain period of time to less than 50%, more preferably to less than 20%, in particular to less than 10% and in the best case to less than 5% by the processes of soil respiration, weathering, aerobic rotting and/or reaction with atmospheric oxygen, wherein the certain period of time can be a selection from the following periods of time: 10 years, 30 years, 100 years, 500 years, 1,000 years, 10,000 years, 100,000 years, >100,000 years.

31. System according to claim 27, comprising devices suitable for extracting or separating at least a portion of the organic nutrients still contained in the residues of the single-stage or multi-stage biomass conversion and/or a portion of the water contained in the residues of the single-stage or multi-stage biomass conversion, wherein these devices preferably consist of a selection from the following devices: spinners, centrifuges, cyclones, decanters, presses, separators, screens, filtration devices, ultrafiltration devices, reverse osmosis devices, similar devices, combinations of these devices, and/or wherein these devices are more preferably suitable for dewatering the residues from the single-stage or multi-stage biomass conversion, preferably to a DS content of >35%, more preferably to a dry substance content of >50% DS and in particular to >60% DS.

32. System according to claim 27, comprising devices suitable for recuperating process water produced in the process and preferably returning it to the process after treatment and/or purification and/or devices suitable for recuperating process heat produced in the process and returning it to the process, wherein the devices for recuperating process heat and/or for heat recirculation preferably comprise components allowing heat exchange which more preferably functions according to the countercurrent principle.

33. System according to claim 27, in which the devices for stabilizing the atmospheric carbon still contained in the conversion residues are preceded by additional devices suitable for pelletizing or briquetting and/or vaporizing, drying, cooling, storing, transporting the conversion residues.

34. System according to claim 27, in which the devices for the single-stage or multi-stage conversion of biomass consist of devices for the anaerobic bacterial fermentation of biomass to biogas and/or bio-methane, which are preferably operated according to the wet fermentation process (wet fermenter), more preferably according to the solid fermentation process (solid fermenter), which are in particular garage fermenters or plug flow fermenters, and in which the at least one garage fermenter is operated with a fermentation cycle of <180 days, preferably with a fermentation cycle of <60 days, more preferably with a fermentation cycle of <35 days, in particular with a fermentation cycle of <21 days and at best with a fermentation cycle of <14 days.

35. System according to claim 29, comprising devices suitable for quenching hot biochar/vegetable coal/biocoke produced by the carbonization devices, preferably with aqueous suspensions selected from slurry, percolate, swill, stillage from ethanol production, liquid residues from anaerobic fermentation, urine, seepage water from silages, process water, processed or purified process water, liquid fermentation mass, permeate, more liquid phase of dehydration, more solid phase of dehydration, any phase of separation, suspensions containing other nutrients and similar suspensions, more preferably with such aqueous suspensions of this selection containing organic nutrients, and in particular process water containing organic nutrients, the organic nutrients of which were previously part of the residues from the single-stage or multi-stage biomass conversion.

36. System according to claim 29, the devices of which for carbonizing conversion residues are suitable for performing both pyrolysis and torrefaction, and/or which comprises devices suitable for loading produced biochar/vegetable coal/biocoke, preferably biochar/vegetable coal/biocoke mixtures and more preferably biochar/vegetable coal/biocoke conversion residue mixtures, with nutrients, for quenching them with water (process water or fresh water), mixing, conveying, warehousing, storing, pelletizing or briquetting them with one another and/or spreading them out on agricultural or forestry land and/or to incorporating them there.

37. System according to claim 27, comprising devices suitable for recuperating, liquefying, purifying, processing, storing, transporting (preferably in liquid aggregate state), delivering to industry, introducing into geological formations, converting into CO.sub.2-based fuel, heating medium or combustion material, performing a combination of these functions, atmospheric carbon dioxide (CO.sub.2) produced in the methods of claims 1 to 26.

38. System according to claim 27, which comprises devices suitable for subjecting the input materials and/or the residues from the single-stage or multi-stage conversion of the biomass into another energy carrier to comminution, preferably chopping or shredding, more preferably a comminution combination consisting of chopping or shredding and grinding, and in particular a comminution combination consisting of bale disintegration, chopping/shredding and grinding, wherein these comminution devices, alone or in combination, are suitable for performing the comminution to an average final particle length of <20 cm, preferably to an average final particle length of <5 cm, more preferably to an average final particle length of <10 mm, in particular to a final particle length of <3 mm and in the best case to a final particle length of <1 mm.

39. System according to claim 27, which comprises devices suitable for subjecting biomass, to a selection of the following treatments before or during the single-stage or multi-stage conversion or residues from the biomass conversion after the single-stage or multi-stage conversion to a selection from the following treatment methods: comminution to a degree of fineness of up to 0.1 mm, soaking/mixing/mashing in cold water or aqueous suspensions, soaking/mixing/mashing in 20° C.-100° C. warm water or aqueous suspensions, biological treatment with fungi, pressurization to >1 bar-500 bar, treatment with >100° C. hot water, treatment with saturated steam, treatment by thermal pressure hydrolysis, steam explosion, treatment by wet oxidation, heating, treatment by extrusion, ultrasonic treatment, treatment by steam reforming, evaporation, sedimentation, crystallization, catalysis, drying, use of polymers, phase separation, particle extraction, combination of a selection of these treatment methods.

Description

7. BRIEF DESCRIPTION OF THE DRAWINGS

[0420] The figures show embodiments and details of the invention, wherein the basic concept of the invention and the scope of protection should not be restricted to the exact forms or details of the embodiments shown and described below. The scope of protection shall also include modifications (extensions and restrictions) which are previously known in the relevant arts and/or obvious to a person skilled in the art.

[0421] FIG. 1 shows a schematic diagram of a complex embodiment of the method and system according to the invention, in which a biomass is selected from many available biomasses, harvested and pre-treated prior to the (first) conversion, wherein the energy carrier generated with the (first) conversion is mixed with other energy carriers, the conversion residue is divided into four partial streams A to D and the conversion residues A to C are dehydrated, wherein the dehydration can be associated with nutrient extraction and releases nutrient-containing process water; after comminution and, if necessary, pelletization of the conversion residues possibly treated in this way, conditions for a chemical-physical stabilization of atmospheric carbon are created in a reaction vessel; as soon as these conditions exist, the atmospheric carbon contained in conversion residues A to C is chemically and physically stabilized, namely A is fully stabilized, B is partially stabilized and C is not stabilized; this (partial) stabilization results in biochar masses E to G, which are quenched with the nutrient-containing process water and loaded with these nutrients; the biochar masses are mixed with one another to form a biochar mixture H which is mixed with untreated conversion residues D to form a biochar conversion residue mixture I; after pelletizing the biochar mixture H or the biochar conversion residue mixture I, the pellets produced are filled into BigBags and distributed via regional interim storage facilities to the farms where they are filled into solid manure spreaders, fertilizer spreaders or slurry distributors. After the application of the biochar mixture or the biochar conversion residue mixture, these are worked into the topsoil of the fields where they can develop their positive effect on the soil and the atmosphere of the earth.

[0422] FIG. 2 shows a further schematic diagram of an embodiment of the method and system according to the invention without the conversion residue D indicated in FIG. 1 and with a first recuperation of atmospheric carbon dioxide (CO.sub.2 I) on the occasion of the (first) conversion of the selected biomass into a produced energy carrier; furthermore, a second recuperation of atmospheric carbon dioxide (CO.sub.2 II) is shown; CO.sub.2 I and CO.sub.2 II are combined, liquefied and geologically sequestered, used as substitutes for fossil CO.sub.2 or used for the production of CO.sub.2-based energy carriers.

8. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0423] For a better understanding of the present invention, reference is made in the following to the embodiments shown in the drawings, which are described using specific terminology. The terminology is consistent, i.e. the respective designations apply to all figures. It should be noted that the scope of protection of the invention shall not be restricted by the designation of the embodiments shown in the drawings. On the contrary, the embodiments and modifications of the embodiments shall also be covered by the claimed protection. Furthermore, certain amendments, additions and other modifications will be obvious to a person of ordinary skill in the art familiar with the invention. Obvious modifications of the method disclosed herein and its embodiments as well as amendments, additions and other modifications of the disclosed system and its embodiments as well as further obvious applications of the invention, which are obvious to a person of ordinary skill in the art, shall be regarded as normal current or future expert knowledge of a person skilled in the relevant art and shall also be protected.

[0424] The features, advantages and details of the invention, which are disclosed in the drawings and claims, can be essential for the further development of the invention, either individually or in any combination. The basic concept of the invention shall not be limited to the exact forms or details of the embodiments shown below. It should also not be limited to a subject matter which would be restricted in comparison to the subjects described in the claims.

[0425] The elements followed by reference signs can indicate both a process and a device as well as the product of a process, if necessary at the same time.

[0426] FIG. 1 shows a schematic diagram of a complex embodiment of the method and system according to the invention, which basically can also only consist of the conversion of biomass 4 by means of suitable devices into a generated energy carrier 5 as well as the generation of suitable conditions for the chemical-physical stabilization 20 of the atmospheric carbon still contained in the conversion residues and the conduction of carbon stabilization 21. These method steps are carried out in each case with suitable devices which are known to a person skilled in the art from the relevant prior art and which are described above, at least in part, and below. Even without sequestration 33 of the biochar or vegetable coal or biocoke produced, stabilization 21 of the atmospheric carbon already ensures that it can no longer react with atmospheric oxygen to form CO.sub.2 or with hydrogen to form CH.sub.4. This decarbonizes the atmosphere of the earth.

[0427] The at least one biomass to be used is selected in a method step 1 from a plurality of available biomasses (see claim 21). Some biomasses are only loaded with low GHG emission quantities up to the production stage of the biomass accumulation, some are even GHG-neutral (e.g. straw resulting from the grain harvest) and some are highly harmful to the environment, such as liquid manure or poultry manure stored outdoors, which emit CH.sub.4 and N.sub.2O. Their early use in a biomass conversion process prevents these GHG emissions, so that early utilization helps to avoid GHG emissions. This GHG avoidance is allocated to the product of the conversion process or is technically linked thereto, so that the utilization of certain farm manures can even lead to a GHG negative initial effect. The selection of one or more suitable biomasses for conversion process 4 can therefore be advantageous.

[0428] The selection 1 is also advantageous for a second reason. Some input materials are not suitable, or only suitable to a limited extent, for C-stabilization 20/21. Liquid input materials, such as fermented slurry, can only be carbonized using the HTC method. This method only provides partially stabilized biochar/vegetable coals, which do not remain stable for centuries or millennia. Therefore, a permanent sequestration with these HTC-coals is not possible (see chapter “Background”). Consequently, it is advantageous to select the input material 1 prior to the (first) conversion of the input material 1 into a generated energy carrier 5 in such a way that its conversion residue can still be used for chemical-physical stabilization that provides permanently stabilized carbon. This is the case with solid or lumpy lignocellulose-containing input materials, such as straw and wood, which are therefore preferably used in the method and system of FIG. 1. Sold or lumpy conversion residues containing straw and wood from a first biomass conversion can, for example, be subjected to pyrolysis, which provides permanently stabilized biochar/vegetable coals or biocoke. This makes a permanent decarbonization of the atmosphere of the earth possible.

[0429] The at least one biomass, which is preferably lignocellulose-containing biomass, more preferably straw, is harvested or collected in a step 2. In this context, harvesting and collection involve the transport of the at least one input material from the point of production to the point of use of the at least one input material. In particular, devices, apparatuses, installations and equipment can be used that use GHG-emission-reduced, preferably GHG-neutral and more preferably GHG-emission-negative fuels, heating mediums and combustion materials. These include, for example, combine harvesters, corn harvesters, tractors, wheel loaders, manitous, trucks, semitrailer tractors and all similar harvesting and transport machines with CNG or LNG drive known from the relevant prior art. These machines can use the energy carrier 5, energy carrier 6, energy carrier mix 7 or energy carrier mix 9 produced according to the method and system of FIG. 1 as fuel, wherein these fuels are GHG-emission-reduced, preferably GHG-neutral and in particular GHG-negative. By using such equipment with such drives and fuels, the GHG footprints and GHG emission values of the generated energy carriers 5, 7 and 9 are reduced, preferably to 0.0 gCO.sub.2-eq/kWh.sub.Hi, more preferably to less than 0.0 gCO.sub.2-eq/kWh.sub.Hi.

[0430] The process 2 can be limited to a collection if the at least one biomass is a by-product, residue or waste. Harvesting is required if the biomass is agricultural or forestry biomass or If it is an agricultural by-product (residue), such as straw. Straw, for example, must usually be pressed into straw bales in swaths after it has been deposited by the combine harvester since loose straw is not suitable for transport. The baling is carried out with tractor-drawn and tractor-driven straw bale presses, which usually achieve a pressing capacity of about 35 tons per hour. Alternatively, the straw deposited in the swath can also be pressed into pellets, highly suitable for transport, already in the field by tractor-drawn pellet presses (pellet harvesters). However, the pressing capacity of the pellet presses is currently only about 5 tons per hour, which blocks valuable tractor and personnel capacity, which is scarce especially during the harvesting campaign. With a bulk density of 600-700 kg/m.sup.3, straw pellets are much more suitable for transport than straw bales, in particular when using the long-distance means of transport rail or ship.

[0431] When using the truck as a means of transport, there is no further increase in transport efficiency at the moment when the load is using up the transport capacity of the truck. This is the case when the straw is compressed into high-pressure bales with a density of about 200 kg/m.sub.3 and the load volume is exhausted.

[0432] In addition to pressing, the straw harvest also includes collecting the straw bales and loading the first means of transport. With collection trucks that are clamped to the straw baling press, a pre-collection can be carried out by accumulating 3-4 straw bales each before they are placed in a group on the stubble field. By placing the bales in groups, the distances travelled or the loading cycles of the loading equipment that load the (first) means of transport used to move the straw bales from the field are reduced.

[0433] In the case of smaller quantities of straw to be harvested, the (first) means of transport usually consists of agricultural trailers available on the farm, in the case of larger farms of low-loader semi-trailers which are mounted on tractor-drawn double-axle mountings or tractor-drawn low-floor trailers. The loading of the means of transport is usually done with front loaders (tractors or so-called manitous), which pick up the bales individually or in pairs and load them onto the means of transport. The loaded straw is transported from the first means of transport to the edge of the field or to the farm where it is unloaded again with front loaders or manitous and piled up outside to straw haystacks or stored in weather-protected warehouses. The route rarely exceeds 10 km. The straw bales can be cuboid or round. Bale collecting trucks are also known from Spain, with which square bales are collected and unloaded at the edge of the field.

[0434] For larger quantities of straw, the (second) means of transport consists of truck-towed trailers or semi-trailers towed by tractors. This means that the semitrailers drive directly onto the field or—if harmful compaction of the soil is to be avoided—at least to the edge of the field. Loading is usually carried out with wheel loaders which have a special grab with which up to 6 square bales can be grabbed at once and loaded onto the (second) means of transport. When so-called high-presses or ultra-high-presses are used, the density of the square bales reaches up to 0.210 t/m.sup.3, which almost fully utilizes the weight loading capacity of the trucks (about 20 t) when the loading volume is fully utilized. The straw can then be transported over several hundred kilometers, as is already the case today, namely from the Magdeburg area to Holland and Belgium, where there is a high demand for straw, for example for mushroom cultivation. Usually, however, the straw is temporarily stored at a regional straw storage facility, protected from arson, before it is transported over long distances. It is advantageous to use in the method and system shown in FIG. 1 the harvesting and transport technology that is used for larger quantities of straw because it is more energy-efficient than the small-sized technology usually used. Thus, harvesting can be carried out with less use of the valuable energy carriers 5, 7 or 9.

[0435] The (first) single-stage or multi-stage biomass conversion 4 can be any type of biomass conversion previously known from the relevant prior art that has the purpose of producing a marketable energy carrier. These include in particular the KIT Bioliq® process, the CLARIANT AG (formerly Süd-Chemie GmbH) Sunliquid® process, the IOGEN process for producing ethanol from lignocellulose-containing biomass, the CHOREN process, the Verbio AG process for producing biogas from straw, the Lehmann process for producing biogas from straw, the Fraunhofer process for producing biogas from biomass, the Jensen & Jensen process for producing biogas from straw, all Hoffmann processes for producing biogas from biomass, all processes by Lutz (Bekon) for producing biogas from biomass, all processes by Schiedermeier (BioFerm) for producing biogas from biomass, all processes by Eggersmann for producing biogas from biomass, all processes for producing ethanol from biomass, all processes for producing FT-fuel from biomass, all processes for producing methanol from biomass, all processes for producing DME from biomass, all other processes for producing fuel from biomass (cf. claim 1).

[0436] The different forms of single-stage or multi-stage biomass conversion 4 are carried out using devices, installations, apparatuses or systems which are previously known from the relevant prior art and which are suitable for this purpose, preferably in order to achieve economies of scale with installations of an industrial scale. More preferably, the devices for the single-stage or multi-stage conversion of biomass can consist of a selection of the following devices: Devices for the anaerobic bacterial fermentation of biomass into biogas and/or bio-methane, devices for the alcoholic fermentation of biomass into bioethanol or ligno-ethanol, devices for the carbonization of biomass into carbonization gas (weak gas), devices for the gasification of biomass into pyrolysis gas and/or pyrolysis slurry, devices for the transesterification of vegetable oils into bio-diesel (FAME), Devices for the hydration of vegetable oils in HVO (mineral oil refineries), devices for refining vegetable oils in HVO (NesteOil process), devices for the gasification/pyrolysis of biomass to process gas, devices for the conversion of biomass-derived process gas into synthesis gas, devices for the synthesis of biomass-derived synthesis gas into a Fischer-Tropsch fuel (FT-diesel, FT-gasoline, FT-kerosene, FT-methanol and the like), devices for the synthesis of methanol from biomass-derived gases, devices for DME synthesis, any combination of these devices (cf. claim 28). Single-stage or multi-stage biomass conversion 4 with biogas installations is particularly preferred, especially with agricultural biogas installations and at best with medium-sized or industrial biogas installations (cf. claim 34). When using these devices, the wet fermentation process in wet fermenters can be used, but also the solid fermentation process in sold fermenters, preferably in garage or plug flow fermenters. If garage fermenters are used, they are operated with a fermentation cycle of <180 days, preferably with a fermentation cycle of <60 days, more preferably with a fermentation cycle of <35 days, in particular with a fermentation cycle of <21 days and at best with a fermentation cycle of <14 days (cf. claim 34).

[0437] Before the (first) single-stage or multi-stage biomass conversion 4, the biomass, which is preferably lignocellulose-containing biomass, especially straw, can be pre-treated (but does not have to be). Conversion 4 is preferably an anaerobic bacterial fermentation carried out in a biogas installation, more preferably a solid fermentation and in particular a fermentation in a garage fermenter (cf. claim 23). Conversion 4 is carried out in devices which are previously known from the relevant prior art and which are suitable for such a conversion. Fermentation in a solid fermentation plant has the advantage that the fermentation residue 10 produced after fermentation is present in a heap (and not in liquid form) and thus after dehydration and/or drying in suitable devices a pyrolysis can be carried out which would only be possible with liquid conversion residues with a very high technical and energetic effort.

[0438] Depending on how long and intensively fermentation 4 is carried out in the at least one biogas installation (wet or solid fermentation installation) (Hydraulic Retention Time HRT), a more or less high conversion efficiency results. Long HRTs lead to desirable high conversion efficiencies and short HRTs to low conversion efficiencies. However, even with a very high conversion efficiency, a certain proportion of the atmospheric carbon contained in the input material always remains in the conversion residue, which is chemically and physically stabilized in suitable facilities according to the invention (cf. claims 1 and 27). In an advantageous embodiment of the invention shown in FIG. 1, the average hydraulic residence time of the fresh mass in the fermenter in the case of anaerobic (bacterial) fermentation is less than 250 days, preferably less than 120 days, more preferably less than 70 days, in particular less than 40 days and at best less than 20 days.

[0439] If straw or wood is used as an input material and pre-treatment 3 is carried out, pre-treatment 3 which is upstream of the conversion 4 can consist of a number of previously known measures which are previously known prior art as are the installations, apparatuses and systems used for this purpose. It is possible, for example, that the straw is subjected to comminution, preferably chopping or shredding, more preferably the comminution combination consisting of chopping or shredding and grinding, and in particular the comminution combination consisting of bale disintegration, chopping/shredding and grinding. In order to achieve a high conversion efficiency in the first conversion 4, it is advantageous to perform multi-stage comminution to an average final particle length of <20 cm, preferably to an average final particle length of <5 cm, more preferably to an average final particle length of <10 mm, in particular to a final particle length of <3 mm and in the best case to a final particle length of <1 mm (cf. claim 24). Pre-treatment of straw extrusion which crush and defiber the straw, and similar processes previously known from the prior art are also possible.

[0440] Before, during or after the method step of the single-stage or multi-stage conversion 4 of the selected biomass 1 into another marketable energy carrier 5, the biomass 1, which is preferably lignocellulose-containing biomass, more preferably straw and/or wood, can be subjected, along with or instead of the above described treatment, to a treatment consisting of an appropriate treatment previously known from the relevant prior art, preferably a selection from the following treatment methods: comminution, soaking/mixing/mashing in cold water or aqueous suspensions including lyes and acids, soaking/mixing/mashing in 20° C.-100° C. warm water or aqueous suspensions including lyes and acids, biological treatment with fungi, pressurization to >1 bar to 500 bar, treatment with >100° C. hot water, treatment with saturated steam, treatment by thermal pressure hydrolysis, treatment by wet oxidation, treatment by extrusion, ultrasonic treatment, treatment by steam reforming, treatment by steam explosion, drying, treatment with process water of any kind, treatment with process heat, treatment with enzymes, combination of a selection of these treatment methods by means of suitable installations, apparatuses or systems previously known from the relevant prior art. The schematic embodiment of FIG. 1 only shows the pre-treatment 3 of input materials ½, although it is understood that the above measures can also be applied to conversion residues 10 and/or to all intermediate products produced during a multi-stage conversion 4. Straw and/or wood, for example, can be subjected to a multi-stage conversion 4 with or without pre-treatment 3, namely fermented in a first fermentation, wherein the fermentation residues from this fermentation are treated according to the above-mentioned treatment methods and the fermentation residues treated in this way are fermented again in at least a second fermentation (cf. claim 25).

[0441] Accordingly, the system shown in FIG. 1 can include devices capable of subjecting biomass ½ to a selection of the following treatment methods before or during conversion 4 or residues 10 after biomass conversion 4: soaking/mixing/mashing in cold water or aqueous suspensions, soaking/mixing/mashing in 20° C.-100° C. warm water or aqueous suspensions, biological treatment with fungi, pressurization to >1 bar-500 bar, treatment with >100° C. hot water, treatment with saturated steam, treatment by thermal pressure hydrolysis, steam explosion, wet oxidation treatment, heating, extrusion treatment, ultrasonic treatment, steam reforming treatment, evaporation, sedimentation, crystallization, catalysis, drying, use of polymers, phase separation, particle extraction, combination of a selection of these treatment methods (cf. claim 39).

[0442] Before, during or after the method step of the single-stage or multi-stage conversion 4 of the selected biomass 1 into another marketable energy carrier 5, the biomass 1, which is preferably lignocellulose-containing biomass, more preferably straw, can be provided with suitable additives previously known from the relevant prior art, preferably with a selection from the following additives: Lime, enzymes, enzyme-containing solutions, fungi, acids, lyes, yeasts, water, recycled process water, purified process water, filtered process water, ultrafiltrated process water, process water subjected to reverse osmosis, treated process water, acid-water mixtures, lye-water mixtures, percolate, silage seepage juices, slurry, micro-organisms, any cereal grain stillage from ethanol production, any residue from the production of ligno-ethanol, any by-product/residue from the production of pyrolysis or synthesis gas, any by-product/residue from FT synthesis, any by-product/residue from DME synthesis, any by-product/residue from methanol synthesis, any sugar beet stillage from ethanol production, combination of two or more of these additives (cf. claim 23). The admixture of the additives is preferably carried out with suitable apparatuses, installations or systems previously known from the relevant prior art.

[0443] At least a portion of the residues from the single-stage or multi-stage biomass conversion 4 (conversion residue 10) is recuperated and made available to the further method steps (cf. claim 22). The conversion residues 10 can in particular be residues from a single-stage or multi-stage anaerobic bacterial fermentation 4 (fermentation residues).

[0444] The energy carrier 5 produced in the process step of single-stage or multi-stage conversion 4 can be a selection of biogas, bio-methane, pyrolysis gas, synthesis gas, bio-diesel, bio-kerosene, Fischer-Tropsch fuel, bio-methanol, DME or bio-ethanol (cf. claim 14).

[0445] Preferably, this energy carrier 5 is processed in such a way that it can be used as fuel, heating medium or combustion material, preferably as a transport fuel, more preferable as a road fuel (cf. claim 14). Conversion 4 is preferably carried out with suitable apparatuses, installations or systems previously known from the relevant prior art. The energy carrier 5 produced can assume a gaseous or liquid aggregate state, i.e. for the liquid aggregate state the energy carrier 5 is liquefied with suitable devices previously known from the relevant prior art.

[0446] In an advantageous embodiment of the invention shown in FIG. 1, after the production, distribution and use of the energy carrier 5 produced, which is preferably a fuel, more preferable a gas fuel and in particular bio-methane, there is a lower amount of greenhouse gas in the atmosphere of the earth than after the production, distribution and use of an equal amount of energy of the compatible fossil counterpart of the energy carrier 5 produced, wherein mineral diesel fuel is the compatible fossil counterpart for all diesel substitutes, mineral fuel for Otto engines (gasoline) the compatible fossil equivalent for all substitutes of fuel for Otto engines, mineral kerosene the compatible fossil equivalent for all kerosene substitutes, natural gas (CNG) the compatible fossil equivalent for all natural gas substitutes, LNG the compatible fossil equivalent for all LNG substitutes, LPG the compatible fossil equivalent for all LPG substitutes and the weighted average of mineral fuel for Otto engines and mineral diesel the compatible fossil equivalent for all other fuels, heating mediums and combustion materials (cf. claim 15).

[0447] In another advantageous embodiment, after the production, distribution and use of the generated energy carrier 5, which is preferably a fuel, more preferably a gas fuel and in particular bio-methane, there is a smaller amount of greenhouse gas in the atmosphere of the earth than before, i.e. the generated energy carrier 5 is GHG-negative (cf. claim 16).

[0448] Preferably, the generated energy carrier 5 is mixed with a compatible sustainable energy carrier 6 to form an energy carrier mix 7, wherein the compatible and sustainably generated energy carrier 6 can come from another conversion process which can have a higher GHG emission value than energy carrier 5. The energy source mix 7 resulting from the mixing is used more preferably as a fuel in traffic. The proportion of energy carrier 5 in the energy carrier mix 7 can be between 0% and 100%, and accordingly the proportion of sustainable energy carrier 6 in the energy carrier mix 7 can be between 100% and 0%. The mixing is preferably carried out with suitable apparatuses, installations or systems previously known from the relevant prior art.

[0449] The mixing of the produced energy carrier 5 with the compatible, sustainably produced energy carrier 6 to form an energy carrier mix 7 is preferably carried out in such a way that after the production, distribution and use of the produced energy carrier mix 7 there is a lower amount of greenhouse gas in the atmosphere of the earth according to life cycle analysis or stoichiometric analysis than after the production, distribution and use of an equal amount of energy of the fossil counterpart of the produced energy carrier mix 7, wherein mineral diesel fuel is the fossil equivalent for all diesel substitutes, mineral fuel for Otto engines (gasoline) is the fossil equivalent for all substitutes for Otto engines, mineral kerosene is the fossil equivalent for all kerosene substitutes, natural gas (CNG) is the fossil equivalent for all natural gas substitutes, LNG the fossil equivalent for all LNG substitutes, LPG the fossil equivalent for all LPG substitutes and the weighted average from mineral fuel for Otto engines and mineral diesel the fossil equivalent for all other fuels, heating mediums and combustion materials (cf. claim 17).

[0450] In an advantageous embodiment, the produced energy carrier 5 is mixed with the compatible, sustainably produced energy carrier 6 in such a way that after the production, distribution and use of the produced energy carrier mix 7 according to life cycle analysis or stoichiometric analysis, a smaller amount of greenhouse gas is present in the atmosphere of the earth than before. This means that the GHG emission value of the energy source mix 7 is GHG negative (cf. claim 18).

[0451] The energy carrier 5 is preferably biogas processed into bio-methane, more preferably straw-gas, which was produced by anaerobic bacterial fermentation at least proportionally from straw-containing and possibly other input materials (farm manure, beet and potato haulms as well as legume waste, wood). More preferably, the compatible sustainable energy carrier 6 is syn-methane, which was produced from wind power and atmospheric CO.sub.2, or is another biogas. In particular, energy carrier 5 and energy carrier 6 are mixed in such a way that after the production, distribution and use of the energy carrier mix according to life cycle analysis or stoichiometric analysis, a lower (measured in tons of CO.sub.2 equivalent) amount of greenhouse gas is present in the atmosphere of the earth than after the production, distribution and use of an equal amount of energy of the fossil equivalent of the energy source mix 7, at best in such a way that after the production, distribution and use of the energy carrier mix 7 there is a smaller amount of greenhouse gas in the atmosphere of the earth than before, i.e. the energy carrier mix 7 produced is GHG negative. In the case of straw-gas, the energy carrier 5 can be mixed with syn-methane 6 in such a way that the resulting mixed gas 7 is GHG neutral (cf. claim 19). The quantity of added syn-methane 6 depends on its GHG value because the higher the GHG value, the lower the syn-ethane 6 quantity that can be admixed. The mixing is preferably carried out with suitable apparatuses, installations or systems previously known from the relevant prior art. The energy source mix 7 can assume a gaseous or liquid aggregate state, i.e. for the liquid aggregate state, the energy carrier 5 produced and the sustainably produced compatible energy carrier 6 are liquefied before or after mixing with suitable devices known from the relevant prior art.

[0452] Preferably, the energy carrier mix 7 and at least one compatible fossil energy carrier 8 can be mixed as the end product to produce an energy carrier mix 9. The energy carrier mix 9 resulting from the mixing is used more preferably as a fuel in traffic. The proportion of energy carrier 7 in the end product 9 can be between 0.1% and 100.0%, and accordingly the proportion of fossil energy carrier 8 in the end product 9 can be between 99.9% and 0.0%. In particular, the energy carrier mix 7 is biogas processed to bio-methane mixed with other biogas or syn-methane 6, at best straw-gas produced from straw-containing input materials mixed with other biogas or syn-methane. The mixing is preferably carried out with suitable apparatuses, installations or systems previously known from the relevant prior art.

[0453] The compatible fossil energy carrier 8 is preferably natural gas or LNG (liquefied natural gas). The mixing of the energy carrier mix 7 and the fossil energy carrier 8 is more preferred in such a way that, according to life cycle analysis or stoichiometric analysis, a lower greenhouse gas amount (measured in tons of CO.sub.2 equivalent) is present in the atmosphere of the earth after the production, distribution and use of the energy carrier mix 9 than after the production, distribution and use of an equal energy amount of the fossil equivalent of the energy carrier mixture 9, more preferably in such a way that after the production, distribution and use of the energy carrier mixture 9 there is a smaller amount of greenhouse gas in the atmosphere of the earth than before, i.e. the generated energy carrier mixture 9 is GHG negative.

[0454] In the case of straw-gas, the energy carrier mix 7 can be mixed with natural gas (CNG) 6 in such a way that the resulting mixed gas is GHG neutral. The quantity of the added natural gas 6 here depends on the GHG emission value of the energy carrier mix 7, because the higher the GHG emission value, the lower the quantity of natural gas 8 that can be admixed.

[0455] The energy carrier mix 9 can assume a gaseous or liquid aggregate state, i.e. for the liquid aggregate state the energy carrier mix 7 produced and the compatible fossil energy carrier 6 are liquefied before or after mixing with suitable devices known from the relevant prior art.

[0456] The conversion residue 10 resulting from the single-stage or multi-stage biomass conversion 4, which is preferably an anaerobic bacterial fermentation, is at least partially recuperated (cf. claim 22). The amount of the resulting conversion residue 10 depends on the conversion efficiency achieved by conversion 4 of the biomass (reference numerals 1 and 2) into the energy carrier 5. If the resulting conversion residues are completely recuperated and the conversion efficiency is e.g. 10%, about 90% of the atmospheric carbon contained in the biogenic input material is still contained in conversion residue 10. If the conversion efficiency with complete recuperation of the conversion residue is e.g. 70%, about 90% of the atmospheric carbon contained in the biogenic input material is still contained in conversion residue 10.

[0457] In the process and system variant shown in FIG. 1, the recuperated proportion of conversion residue stream leaving the method step of single-stage or multi-stage biomass conversion is divided in the method and system variant shown in FIG. 1 in an additional method step 11 into up to four partial streams A to D (reference signs 12 to 15), namely into the first partial stream “production of stabilized pyrolysis coal”, into the second partial stream “production of partly stabilized torrefaction or HTC coal”, into the third partial stream “production of unstabilized biochar/vegetable coal/biocoke” and into the fourth partial stream “non-carbonized conversion residues” (cf. claim 9). The purpose of this division is to obtain a biochar/vegetable coal mixture or a biocoke mixture that is better suited to forest and agricultural soils than biochar/vegetable coal that consists only of fully stabilized, partially stabilized or unstabilized atmospheric carbon—although these options shall not be excluded. In order to avoid repetitions, reference is made in this respect to the above descriptions and explanations.

[0458] The partial streams A to D (RS 12 to 15) can each have a share of 0% to 100% of the total stream, i.e. each partial stream 12 to 15 can represent the total stream as well as zero and each share in between (cf. claim 9). The partial stream A with reference sign 12 “production of stabilized pyrolysis coal” preferably has a share of >1% of the total stream, more preferably a share of >25%, in particular a share of >50% and in the best case a share of >75% (cf. claim 9). The higher the proportion of fully stabilized carbon in the biochar/vegetable coal mixture, the greater the permanent decarbonization effect and the resulting effect on the GHG emission values of the energy carriers 5, 7 and 9. The partial streams A to D can be divided using a switch that divides the conversion residue stream 10 leaving conversion 4 into various suitable conveyors, such as lines, conveyor belts, chutes, elevators, etc. (not shown) or containers.

[0459] In the method steps following stream distribution 11, the respective partial stream is carried out by means of suitable installations, apparatuses or systems, which is indicated by the partial stream designation (cf. claim 9). This means that the partial stream A (RS 12) serves for the full stabilization of atmospheric carbon, wherein this full stabilization is carried out in method steps 20 and 21, preferably by means of pyrolysis, more preferably by means of high-temperature pyrolysis and in particular by means of high-temperature pyrolysis, which is carried out after a slowly carried out heating. Biochar/vegetable coal with fully stabilized atmospheric carbon advantageously increases the permanent humus content of the soil.

[0460] Accordingly, partial stream B (reference sign 13) serves for partial stabilization of atmospheric carbon in method steps 20 and 21, preferably by means of HTC, more preferably by means of low-temperature pyrolysis (torrefication) and in particular by means of low-temperature pyrolysis (torrefication) which is carried out after slow heating. Biochar/vegetable coal with partially stabilized atmospheric carbon increases the nutrient humus content of the soil in an advantageous way.

[0461] Partial stream C (reference numeral 14) is used to produce biochar/vegetable coal containing unstabilized atmospheric carbon. For this purpose, inter alia any carbonization process can be used, including pyrolysis, which must be carried out only briefly and/or aggressively enough (very fast heating, very high reaction temperatures). Biochar/vegetable coal with unstabilized atmospheric carbon increases the OPS or OSS content of the soil in an advantageous way.

[0462] The partial stream D (RS 15) serves to advantageously increase the OPS or OSS content of the soil. It is comparable with conversion residues 10, which are applied directly and without after-treatment as fertilizer on agricultural land after a single-stage or multi-stage conversion 4. Such conversion residues are e.g. fermentation residues from anaerobic bacterial fermentation or stillage from the alcoholic fermentation of biomass to bio-ethanol.

[0463] The up to four products (biochar masses E to G and conversion residue D), which may or may not be produced in the method steps following conversion residue division 11, can generally be processed or treated in parallel or in series with the respective installations and apparatuses. In the case of serial processing, the unprocessed partial streams are conveyed to suitable intermediate storage facilities (not shown) by means of suitable conveyor technology (not shown) which is previously known from the relevant prior art, and stored until further processing is started. It is thus possible to first carry out high-temperature pyrolysis with one and the same device for C-stabilization and then torrefaction with a significantly lower reaction temperature and/or a significantly shorter reaction time. Devices which are suitable for high reaction temperatures are usually also suitable for lower reaction temperatures. The same applies to the parameters heating rate, reaction time and reaction pressure.

[0464] After dividing the residual conversion stream 10 into the partial streams A to D (reference signs 12 to 15), the partial streams A to C pass through three optional method steps, namely dehydration/nutrient extraction 16, disintegration 18 and pelletization/briquetting 19. However, such treatment is not absolutely necessary; the objective is also achieved if the conversion residues 10 or partial streams 12 to 14 do not pass through method steps 16 to 19 and are led straight to method steps 20 and 21. The division is preferably carried out with a suitable switch or the like which is previously known from the relevant prior art.

[0465] In an advantageous embodiment (not shown in FIG. 1) of the method and system shown in FIG. 1, the residual conversion partial streams A to D (RS 12 to 15) generated by means of division 11 can be stored in a silo, container, bunker or similar devices previously known from the relevant prior art until there is a need for them. This demand can be based on downstream dehydration/nutrient extraction 16, downstream desintegration 18, downstream pelleting/briquetting 19, downstream C-stabilization 20/21 or downstream mixing 27.

[0466] In the method step of dehydration/nutrient extraction 16, the conversion residues 12 to 14 are dewatered by means of suitable installations, apparatuses or systems previously known from the relevant prior art. Preferably, devices are included which are capable of extracting or separating at least a portion of the organic nutrients still contained in the residues of the single-stage or multi-stage biomass conversion or at least a portion of the water still contained in the residues of the single-stage or multi-stage biomass conversion, which devices can more preferably consist of a selection from the following devices: soaking, mixing, mashing and similar devices, spinners, centrifuges, cyclones, decanters, presses, separators, screens, filtration devices, ultrafiltration devices, reverse osmosis devices, similar devices, combination of these devices (cf. claim 31).

[0467] Dewatering 16 is advantageous because the downstream stabilization of the atmospheric carbon functions the better and more effective, the higher the dry substance content of the biomass to be treated in method steps 20 and 21. In an advantageous embodiment of the method shown in FIG. 1, dewatering is therefore carried out in such a way that the dry substance content (DS content) of the resulting, more solid phase is >35%, preferably >50% DS, more preferably >60% DS (cf. claim 4). For this purpose, devices previously known from the relevant prior art are used, preferably those which are suitable for extracting or separating at least a portion of the water contained in the conversion residues 12 to 14, wherein these devices more preferably consist of a selection from the following devices: Spinners, centrifuges, cyclones, decanters, presses, separators, screens, filtration devices, ultrafiltration devices, reverse osmosis devices, similar devices, combinations of these devices. These dewatering devices are preferably suitable for dewatering the conversion residues 12 to 14 from the single-stage or multi-stage biomass conversion 4, preferably to a DS content of >35% DS, more preferably to a DS content of >50% DS and in particular to >60% DS (cf. claim 31).

[0468] In addition to the more solid phase, the product of dewatering 16 is a more liquid phase, which is referred to here as process water 17. “More solid” in this context means that the solid phase also contains water just as the “more liquid” phase contains dry substance. This means that the DS content of the more solid phase is not 100% but—unless otherwise stated—only higher than the DS content of the more liquid phase.

[0469] The process water 17 can be used to quench, if necessary, the biochar/vegetable coal coming from the C-stabilization or the biocoke coming from the C-stabilization, which is usually very hot. This is done in method step 25. However, it can also be used to replace (fresh) water requirements elsewhere in the method, e.g. In method step 3 (e.g. pretreatment by soaking in water or aqueous suspensions) and/or in method step 4 (e.g. anaerobic bacterial fermentation in a wet fermenter) and/or in method step 19 (evaporation of conversion residues 12 to 14 to be pelletized or briquetted).

[0470] The system shown in FIG. 1 can comprise devices which are previously known from the relevant prior art and are suitable for recuperating process water produced in the method and supplying it to other system components (lines, containers, bunkers, reservoirs, pumps, etc.), preferably after processing or purification of the recuperated process water in corresponding devices previously known from the relevant prior art, more preferably after processing or purification of the recuperated process water by means of a selection from the following devices: spinners, centrifuges, cyclones, decanters, presses, separators, screens, filtration devices, ultrafiltration devices, reverse osmosis devices, similar devices, combinations of these devices (cf. claims 31 and 32).

[0471] The process water 17 usually contains valuable organic nutrients to a technically relevant extent. After the (first) single-stage or multi-stage biomass conversion 4, which is preferably an anaerobic fermentation, the (organic) nutrients contained in the biogenic input material are still largely present, i.e. they are contained in the recuperated conversion residue 10 or in the conversion residue partial streams 12 to 15. Most of them are in solution. This means that the process water 17 leaving the conversion residues 12 to 14 can be aqueous suspensions enriched with (organic) nutrients. The composition of these nutrients corresponds exactly to that of the composition of the nutrients removed from the topsoil during biomass cultivation or biomass growth. As shown above, it is advantageous for the field topsoil if the applied biochar/vegetable coal is loaded with nutrients. To avoid repetitions, reference is made to the relevant sections of the above Illustrations. Since the most of the nutrients contained in the conversion residues 12 to 14 are destroyed and/or lost during chemical-physical stabilization 20/21 of the atmospheric carbon still contained in the conversion residues 12 to 14, it is advantageous to extract at least part of these nutrients from the conversion residues prior to C-stabilization by means of suitable installations, apparatuses or systems previously known from the relevant prior art and to then use them to load the biochar/vegetable coal 22 to 24 produced (cf. claim 31). The biochar/vegetable coals are loaded with nutrients in method step 25 (see below).

[0472] According to the invention, the organic nutrients still contained in the residues of the single-stage or multi-stage biomass conversion 4 are therefore at least partially removed, prior to the chemical-physical treatment of the conversion residues 12 to 14, from these conversion residues by means of suitable apparatuses, installations or systems previously known from the relevant prior art, preferably together with process water 17, more preferably by a selection from the methods of spinning, decanting, pressing, separation, filtration, reverse osmosis, addition of polymers, combination of these method steps and in particular with corresponding suitable apparatuses and installations (cf. claim 4).

[0473] According to the invention, the process water 17 obtained, which is preferably an aqueous suspension that contains organic nutrients, is returned to the process, more preferably by means of suitable apparatuses, such as lines, containers, tanks, bunkers and pumps (cf. claim 4) and in particular after purification of inhibitors or residual materials.

[0474] The conversion residues 12 to 14, which may have been dehydrated in method step 16 and/or from which organic nutrients may have been extracted in the same method step 16, can be disintegrated in an optional method step 18 using suitable disintegration apparatuses previously known from the relevant prior art (cf. claim 38), namely to an average particle length of 0.01 mm to 300 mm, preferably to an average particle length of 0.1 mm to 100 mm, more preferably to average particle lengths of 1.0 mm to 30 mm and in particular to average particle lengths of 1.5 mm to 20 mm. Disintegration can be advantageous because the biochar/vegetable coals 22-24 produced can be better distributed on (arable) soil and/or better incorporated into (arable) soil. A high degree of fineness is particularly advantageous if the biochar/vegetable coals 22-24 produced shall be mixed with slurry, with or without nutrient loading, in order to reduce or prevent unpleasant odors from the slurry and/or to reduce environmentally harmful N.sub.2O emissions resulting from the spreading of the slurry. For this purpose of easier distribution by means of a slurry distributor, disintegration 18 can also be carried out later in the process, for example immediately after C-stabilization 20/21, immediately after quenching/loading with nutrients 25, immediately after mixing to a biochar mixture H 26 or immediately after mixing to a biochar conversion residue mixture 27.

[0475] The optional disintegration 18 with suitable apparatuses previously known from the relevant prior art can be advantageous for a second reason, namely as a preparatory measure for a possibly downstream pelletization or briquetting 19. If the chemical-physical stabilization 20/21 is to consist of carbonization of the conversion residues 12 to 14 and these consist of pyrolysis, pyrolysis methods and apparatuses can be used which can only pyrolyze input materials that are lumpy or cut into lumps. In order to be able to use these methods and apparatuses, pelletization/briquetting of the conversion residues 12 to 14 is required. This in turn can require comminution of the conversion residues 12 to 14. If the comminution has not already taken place during the pretreatment 3 to the degree of fineness required for pelleting/briquetting, the comminution must then take place at the latest before method step 19 (pelleting/briquetting).

[0476] The optional disintegration 18 with suitable apparatuses previously known from the relevant prior art can be advantageous for a third reason, namely as a preparatory measure for the downstream C-stabilization 20/21. If the chemical-physical stabilization 20/21 is to consist of a carbonization of the conversion residues 12 to 14 and the latter of a pyrolysis, pyrolysis processes and apparatuses can be used which can only pyrolyze input materials with a certain degree of fineness. The PYREG 500 pyrolysis system from Pyreg GmbH currently only processes input materials that do not exceed a certain particle length.

[0477] The optional pelletizing/briquetting 19 can be necessary if the chemical-physical stabilization 20/21 shall consist of a carbonization of the conversion residues 12 to 14 and the latter of a pyrolysis. In this case, pyrolysis processes and apparatuses can be used which can only pyrolyze materials that are lumpy or cut into lumps. In order to be able to use these methods and apparatuses, pelletizing/briquetting 19 of the conversion residues 12 to 14 can be necessary.

[0478] Accordingly, the system of FIG. 1 can include devices which are previously known from the prior art and can pelletize or briquette the conversion residues prior to C-stabilization 21 and/or perform the associated sub-functions, namely to vaporize or dry the mass to be pelleted/briquetted, if necessary, and to cool, store and transport the pellets/briquettes produced (cf. claim 33).

[0479] The generation of conditions allowing at least partial chemical-physical stabilization of the atmospheric carbon still present in the residues of the (first) single-stage or multi-stage biomass conversion (digestion, fermentation, pyrolysis or synthesis residues) (RS 20) can refer to any methods and apparatuses previously known from the relevant prior art for the chemical-physical carbon stabilization. In the case of carbonization of the (possibly pre-treated or post-treated) conversion residues 12 to 14, this method step 20 can include the selection of the carbonization process, the selection of the aggregate state of the mass to be carbonized, the selection of the reaction vessel (reactor), the heating to a certain reaction temperature, the heating to reaction temperature in a certain period, the conduction of the reaction for a certain (period of) time, pressurization of the reaction mass, a certain kind of pre-treatment of the reaction mass, the kind of cooling the reaction product, another way of post-treatment of the reaction product and the selection of the appropriate devices. The execution of these parameters depends on the partial conversion stream 12 to 14 or the type of biocoal mass E to G (RS 22 to 24) to be used, as described below in the comment on step 21.

[0480] In a preferred embodiment of the method shown in FIG. 1, the conditions of method step 20 and/or the implementation of method step 21 are selected or set in such a way that the atmospheric carbon still contained in the conversion residues 12 and 14 is at least partially stabilized such that it is degraded (mineralized) within a certain period of time by less than 30%, preferably less than 20%, in particular less than 10% and in the best case less than 5% by the processes of soil respiration, weathering, aerobic rotting and/or reaction with atmospheric oxygen, wherein the certain period of time can be a selection from the following periods of time: 10 years, 30 years, 100 years, 500 years, 1.000 years, 10,000 years, 100,000 years, >100,000 years (cf. claim 2).

[0481] Accordingly, the system shown in FIG. 1 comprises devices which are previously known from the relevant prior art and can carbonize the conversion residues 12 and 13 in such a way that the carbon content of the resulting biochar masses 22 and 23 is degraded (mineralized) within a given period of time by less than 50%, preferably less than 20%, more preferably less than 10% and in particular less than 5%, by the processes of soil respiration, weathering, aerobic rotting and/or reaction with atmospheric oxygen, wherein the given period of time can be a selection from the following periods of time: 10 years, 30 years, 100 years, 500 years, 1.000 years, 10,000 years, 100,000 years, >100,000 years (cf. claim 30).

[0482] This degradation resistance is achieved in the case of carbonization of the conversion residues 12 and 13 when the molar H/C ratio of the produced biochar/vegetable coal/biocoke 22 and 23 is <0.8, preferably <0.6, or when its molar O/C ratio is <0.8, preferably <0.4. In particular, this degradation resistance is achieved when, in the case of carbonization, the molar H/C ratio of the biochar/vegetable coal/biocoke 22 and 23 produced is <0.8, preferably <0.6, and when its molar O/C ratio is <0.8, preferably <0.4. In an advantageous embodiment of the method and system described in FIG. 1, the conditions of method step 20 are therefore selected or set such that the molar H/C ratio of the biochar/vegetable coal/biocoke 22 and 23 produced is <0.8, preferably <0.6, and/or its molar O/C ratio is <0.8, preferably <0.4 (cf. claim 6).

[0483] These basic results can be achieved by selecting a particular carbonization process and/or keeping the reaction temperature relatively high and/or by heating to reaction temperature for a relatively long time, i.e. relatively slowly. In an advantageous embodiment of the method and system of FIG. 1, the conditions for the chemical-physical treatment of the conversion residues (RS 20) are therefore preferably set in such a way that the thermal or thermo-chemical carbonization of the conversion residues 12 and 13 (possibly treated according to 16, 18 or 19) to form biochar/vegetable coal/bio-coke is carried out by a selection from the following thermo-chemical carbonization processes: Pyrolysis, carbonization, torrefaction, hydrothermal carbonization (HTC), vapothermal carbonization, gasification and any combination of these treatment methods. This carbonization is preferably carried out by pyrolysis or torrefaction.

[0484] Accordingly, the system shown in FIG. 1 comprises devices previously known from the relevant prior art for the carbonization of conversion residues, preferably those suitable for pyrolysis and/or torrefaction (cf. claim 36).

[0485] The fundamental results listed above can also be achieved by the physico-chemical stabilization of atmospheric carbon by carbonization of the conversion residues 12 to 14 under oxygen deficiency at reaction temperatures of 100° C.-1600° C., preferably at reaction temperatures of 200° C.-1,200° C., more preferably at reaction temperatures of 300° C.-1,000° C., in particular at reaction temperatures of 350° C.-1,000° C. and in the best case at reaction temperatures of 400° C.-900° C. (cf. claim 20). Accordingly, the system of FIG. 1 comprises suitable devices previously known from the relevant prior art for the carbonization of conversion residues, preferably those suitable for ensuring reaction temperatures of 100° C.-1600° C., preferably reaction temperatures of 200° C.-1,200° C., more preferably reaction temperatures of 300° C.-1,000° C., in particular reaction temperatures of 350° C.-1,000° C. and in the best case reaction temperatures of 400° C.-900° C. (cf. claim 36).

[0486] The conversion residues A (RS 12) are preferably subjected to pyrolysis, more preferably to high-temperature pyrolysis, wherein the proportion of the conversion residues A in the total recuperated conversion residue stream 10 preferably has a proportion of >1%, more preferably >50% and in particular >75%.

[0487] The conversion residues B (RS 13) are preferably subjected to low-temperature pyrolysis, HTC or torrefaction, wherein the proportion of the conversion residues B in the total recuperated conversion residue stream 10 preferably has a proportion of <99%, more preferably <50%, in particular <25% and at best of <10%.

[0488] These basic results listed above can also be achieved by heating the conversion residue 12 to 14 to be treated to reaction temperature for longer than 1 second, preferably longer than 10 minutes, more preferably longer than 50 minutes and in particular longer than 100 minutes (cf. claim 20). The less aggressive conditions for C-stabilization 20 lead to better or more complete outgassing of conversion residues 12 to 14, leaving a firmer and less reactive carbon backbone behind, which in turn results in higher degradation resistance.

[0489] These fundamental results listed above can also be achieved in that the conversion residues 12 to 14 (possibly treated according to 16, 18 or 19) have the lowest possible residual water content. In an advantageous embodiment of the method shown in FIG. 1, dehydrated (dewatered) conversion residues 12 to 14 are therefore used in method steps 20/21 because carbonization by pyrolysis or torrefaction functions better in the sense of the objective of “permanent C-stabilization”, the lower the residual water content of the biomass treated in method step 21. Some pyrolysis installations, for example, require dewatering to at least 50% dry substance (DS). The conditions for C-stabilization 20 are preferably set so that the dewatering of the conversion residues 12 to 14 used for this purpose is carried out to >35% DS, more preferably >50% DS and in particular >60% DS (cf. claim 5).

[0490] In a preferred embodiment of the method shown in FIG. 1, the conditions of method step 20 are selected or set in such a way that the loss of atmospheric carbon which inevitably occurs during at least partial chemical-physical stabilization of the conversion residues is a maximum of 99%, preferably a maximum of 60%, more preferably a maximum of 40% and in particular a maximum of 30%. This can be achieved inter alia by heating the conversion residues 12 to 14 to be treated to reaction temperature for longer than 1 second, preferably longer than 10 minutes, more preferably longer than 50 minutes and in particular longer than 100 minutes (see above; cf. claim 20). This can also be achieved by a relatively long reaction time, preferably longer than 1 second, more preferably longer than 60 minutes, in particular longer than 240 minutes and at best longer than 600 minutes.

[0491] The devices of generating conditions allowing at least partial chemical-physical stabilization of the atmospheric carbon still present in the biomass conversion residues can include any devices known from the relevant prior art capable of carrying out chemical-physical treatment of such residues. They preferably include devices for the thermal or thermo-chemical carbonization of conversion residues 12 to 14 to form biochar/vegetable coal/biocoke 22 to 24, more preferably they include a selection from the following devices for the thermo-chemical carbonization of biomass to form biochar/vegetable coal/biocoke: pyrolysis devices, carbonization devices, torrefaction devices, hydrothermal carbonization (HTC) devices, vapothermal carbonization devices, gasification devices, any combination of these devices, wherein the devices for carbonizing the conversion residues are preferably suitable for carrying out the carbonization under oxygen deficiency and/or at reaction temperatures of 100° C.-1600° C., more preferably at reaction temperatures of 200° C.-1.200° C., in particular at reaction temperatures of 300° C.-1,000° C., in an even better case at reaction temperatures of 350° C.-950° C. and in the best case at reaction temperatures of 400° C.-900° C. (cf. claim 29).

[0492] In an advantageous embodiment of the system shown in FIG. 1, the devices for the generation of conditions allowing at least partial chemical-physical stabilization of the atmospheric carbon still contained in the residues of the biomass conversion are operated in such a way that the carbon fraction of the produced biochar/vegetable coals or the biocoke produced is degraded (mineralized) within a given period of time by less than 50%, more preferably less than 20%, in particular less than 10% and in the best case less than 5% by the processes of soil respiration, weathering, aerobic rotting and/or reaction with atmospheric oxygen, wherein the given period of time can be a selection from the following periods of time: 10 years, 30 years, 100 years, 500 years, 1,000 years, 10,000 years, 100,000 years, >100,000 years.

[0493] Once the conditions for C-stabilization have been set as desired in method step 20, C-stabilization 21 is carried out. The way in which the atmospheric carbon contained in conversion residues 12 to 14 is stabilized can be part of the conditions set in method step 20, i.e. method steps 20 and 21 are closely linked. For example, the rate of heating of the conversion residues 12 to 14 can be both a parameter for creating conditions for C-stabilization 20 and a parameter for performing C-stabilization 21. If the heating of the conversion residues 12 to 14 to be treated to reaction temperature falls under method step 21, it also takes longer than 1 second, preferably longer than 10 minutes, more preferably longer than 50 minutes and in particular longer than 100 minutes. The reaction time parameter also plays a role in both method step 20 and method step 21. C-stabilization 21 is therefore preferably carried out over a period of time longer than 1 second, more preferably longer than 60 minutes, in particular longer than 240 minutes and at best longer than 600 minutes.

[0494] In an advantageous embodiment of the method and system shown in FIG. 1, C-stabilization 20/21 is carried out under pressure, preferably at a reaction pressure of >1 bar, more preferably >5 bar and in particular >10 bar.

[0495] The method according to the invention is the more efficient in terms of a GHG emission reduction of the generated energy carrier 5 the lower the loss of (atmospheric) carbon during the C-stabilization 21. The chemical-physical stabilization of the atmospheric carbon contained in the conversion residues 12 to 14 or the carbonization of the conversion residues 12 to 14 is therefore preferably carried out in such a way that the occurring loss of atmospheric carbon based on the state before C-stabilization conversion residue carbonization is a maximum of 99%, more preferably a maximum of 60%, in particular a maximum of 40% and at best a maximum of 30% (cf. claim 3). As stated above, this can be achieved by slow heating to reaction temperature and/or a high reaction temperature and/or a long reaction time.

[0496] During the application of the produced biochar/vegetable coal according to the invention or the produced biocoke in the soil, not only the (stabilized) carbon content in the biochar/vegetable coal has an effect but also the entire biochar/vegetable coal including the other substances contained in it that are not made of carbon. Accordingly, the consumers of the biochar/vegetable coals produced primarily consider the total quantity purchased from the producer or applied per hectare. It is therefore advantageous in terms of a maximum output of biochar/vegetable coal or biocoke if the loss of dry substance occurring during carbonization (RS 21) of the conversion residues 12 to 14 is a maximum of 99%, more preferably a maximum of 60%, in particular a maximum of 40% and at best a maximum of 30% (cf. claim 6).

[0497] The biochar/vegetable coals 22 to 24 or biocoke produced according to the method shown in FIG. 1 are all the more valuable the higher their carbon content is. In an advantageous embodiment of the example of the method according to the invention shown in FIG. 1, C-stabilization 21 is therefore carried out in such a way that the carbon content of the produced biochar/vegetable coal or the produced biocoke is at least 20%, preferably at least 40%, more preferably at least 60%, in particular at least 70% and in the best case at least 80% (cf. claim 6).

[0498] It goes without saying that the devices used for carrying out C-Stabilization 21 are suitable for this purpose.

[0499] C-stabilization 21 is performed in different ways, depending on the conversion residue partial stream. The conversion residue partial stream A (RS 12) is processed in such a way that the atmospheric carbon still contained in the conversion residue is stabilized as completely and permanently as possible under the secondary conditions of the lowest possible carbon loss. At the same time, the dry substance loss of the conversion residue 12 shall be as low as possible and the carbon content of the produced biochar mass 22 as high as possible. This can be achieved by carbonizing the conversion residue partial stream A (RS 12), wherein this carbonization 21 is preferably carried out by pyrolysis or torrefaction, more preferably by high-temperature pyrolysis and in particular by high-temperature pyrolysis which is carried out after slow heating. The conversion residue partial stream A (reference sign 12) is preferably exposed to a temperature of 150° C.-1,600° C. under oxygen deficiency, more preferably to a temperature of 500° C.-1,000° C. and in particular to a temperature of 600° C.-900° C. Preferably the reaction mass is exposed to the reaction temperature for more than 1 second, more preferably for more than 50 minutes and in particular for more than 500 minutes. Preferably, the molar H/C ratio of the produced, highly C-containing biochar/vegetable coals E (RS 22) is <0.8, more preferably <0.6, and/or its molar O/C ratio is <0.8, more preferably <0.4.

[0500] Biochar/vegetable coal E (RS 22) with fully stabilized atmospheric carbon increases the permanent humus content of the soil in an advantageous way with appropriate application because the atmospheric carbon contained in biochar/vegetable coal E can no longer react with atmospheric oxygen to form CO.sub.2 or with hydrogen to form CH.sub.4 for centuries and millennia.

[0501] Partial stream A (RS 12) preferably contains lignocellulose, more preferably wood and in particular straw. If it contains straw, the variant of the method according to the invention that is disclosed in FIG. 1 allows access to those ⅔ of the annual straw growth that had to remain in the field until now to secure the humus content of the soil.

[0502] The conversion residue partial stream B (RS 13) treated on the basis of C-stabilization 21 is processed in such a way that the atmospheric carbon still contained in the conversion residue is partially stabilized under the secondary conditions of the lowest possible carbon loss. At the same time, the dry mass loss of the conversion residue 13 shall be as low as possible and the carbon content of the produced biochar mass 23 as high as possible.

[0503] This can be achieved by carbonizing the conversion residue partial stream B (RS 13), wherein this carbonization 21 is preferably carried out by low-temperature pyrolysis or torrefaction, more preferably by hydrothermal carbonization HTC and in particular by low-temperature pyrolysis or torrefaction, which is carried out after rapid heating. Partial stabilization can also be achieved by the reaction parameters of a pyrolysis being aggressive, i.e. the heating rate to reaction temperature is rapid, the reaction temperature is relatively low and/or the reaction duration is relatively short. The conversion residue partial stream B (RS 13) is preferentially exposed under oxygen deficiency to a reaction temperature which is lower than the reaction temperature used for partial stream A (RS 12). The reaction mass is preferably exposed to the reaction temperature for a shorter period of time than the reaction time used for partial stream A (RS 12). Preferably, the molar H/C ratio of the produced, highly C-containing biochar/vegetable coals F (reference sign 23) is higher than that of the biochar/vegetable coals E (reference sign 22). Preferably, the molar O/C ratio of the produced, highly C-containing biochar/vegetable coals F (RS 23) is higher than that of the biochar/vegetable coals E (RS 22). Biochar/vegetable coal F (RS 23) with partially stabilized atmospheric carbon increases the nutrient humus content of the soil in an advantageous way with appropriate application because the atmospheric carbon contained in the biochar/vegetable coal F can no longer react with atmospheric oxygen to form CO.sub.2 or with hydrogen to CH.sub.4, at least proportionally for decades.

[0504] The conversion residue partial stream C (RS 14) treated on the basis of C-stabilization 21 is processed in such a way that the atmospheric carbon still contained in the conversion residue is not stabilized or is hardly stabilized at al under the secondary conditions of the lowest possible carbon loss. At the same time, the dry mass loss of the conversion residue 14 shall be as low as possible and the carbon content of the produced biochar mass 24 as high as possible. This can be achieved by carbonizing the conversion residue partial stream C (RS 14), wherein this carbonization 21 is preferably carried out by means of only short low-temperature pyrolysis or torrefaction, more preferably by means of short and/or low-pressure hydrothermal HTC carbonization and in particular by means of short low-temperature pyrolysis or torrefaction, which is carried out after very rapid heating. Non-stabilization can also be achieved by the reaction parameters of a pyrolysis being very aggressive, i.e. the heating rate to reaction temperature is very fast, the reaction temperature is very low and/or the reaction time is very short. The conversion residue partial stream C (RS 14) is preferably exposed under oxygen deficiency to a reaction temperature which is lower than the reaction temperature used for partial stream B (RS 13). Preferably, the reaction mass is exposed to the reaction temperature for a shorter period of time than the reaction time used for partial stream B (RS 13). Preferably, the molar H/C ratio of the produced, highly C-containing biochar/vegetable coals G (RS 24) is higher than that of the biochar/vegetable coals F (RS 23). Preferably, the molar O/C ratio of the produced, highly C-containing biochar/vegetable coal G (RS 24) is higher than that of the biochar/vegetable coals F (RS 23). Biochar/vegetable coal G (RS 24) with unstabilized atmospheric carbon increases the OPS or OSS content of the soil in an advantageous way with appropriate application because the atmospheric carbon contained in biochar/vegetable coal G is used as food or energy supplier for the soil flora and fauna at least proportionally for years.

[0505] The product of method step 21 (carrying out C-stabilization) are thus the biochar masses (BCM) 22 to 24. These have different properties as described above. Preferably, these BCM 22 to 24 are produced at least proportionally from straw-containing conversion residues (cf. claim 11).

[0506] The application of fresh, untreated biochar/vegetable coal or fresh, untreated biocoke can lead to the effect of temporary nitrogen immobilization and/or immobilization of other micro- and macronutrients, in particular if the biochar/vegetable coal or biocoke has been produced at low temperatures and/or by the HTC process. As shown above, this effect is due to inter alla the binding of the NH.sub.4 ion and the resulting reduction of nitrification and increased soil respiration. In order that the fresh biochar/vegetable coals or the fresh biocoke 22 to 24 does not remove any nutrients from the topsoil after incorporation thereinto and immobilizes them, the biochar masses E to G produced are enriched in method step 25 (quenching/loading with nutrients) even before they are mixed to a biochar mixture H with exactly the same organic nutrients contained in the cereal plant (the enrichment with organic nutrients can also take place immediately after their mixing to a biochar mixture H).

[0507] Method step 25 preferably involves loading with nitrogen compounds, more preferably enrichment with organic nitrogen compounds. This prevents any (short-term) N-immobilization that may occur during method step 34.

[0508] The loading of the biochar masses E to G (RS 22 to 24) with nutrients can be BCM-specific by quenching the hot torrefied or pyrolyzed biochars/vegetable coals/biocokes separately with process water 17, which was extracted from the conversion residues 12 to 14 in method step 16, preferably together with nutrients, more preferably with the very nutrients that have previously been lost to the soil on which the biochars/vegetable coals are applied by the previous cultivation of the biomass from which the biochars/vegetable coals originate. Optionally, the process water 17 and/or the nutrients extracted from conversion residues 12 to 14 in method step 16 can be supplemented or replaced in this method step 25 by quenching or mixing the biomass coals 22 to 24 with a selection from the following nutrient-containing aqueous suspensions: slurry, percolate, swill, liquid residues from anaerobic fermentation, stillage from ethanol production, urine, seepage water from silages, process water (possibly processed or purified), liquid fermentation mass, permeate, more liquid phase of dehydration, more solid phase of dehydration, any phase of separation, suspensions prepared with mineral fertilizers, suspensions containing other nutrients and similar suspensions (cf. claim 8).

[0509] The loading of the biochar masses E to G (RS 22 to 24) with nutrients or the quenching of the biochar masses E to G (RS 22 to 24) with process water 17 is carried out with suitable devices which are previously known from the relevant prior art, preferably with tanks, containers and mixing devices (cf. claims 35 and 36).

[0510] If the amount of heat contained in the hot biochar/vegetable coals/bio coke 22 to 24 is less than the amount of heat required to evaporate the water supplied for quenching (only the water evaporates during quenching, the organic nutrients dissolved in the water remain in the biochar/vegetable coal mixture), the biochar/vegetable coals/biocoke 22 to 24 or the biochar/vegetable coal mixture H 26 become wet again, otherwise they remain dry. Preferably, only enough liquid (process water 17 or fresh water) is used for quenching 25 to keep the quenched biochar/vegetable-coal/biocoke dry.

[0511] If necessary, and if necessary at all, the quenched biochar/vegetable coals 22 to 24 can be dried (not shown in FIG. 1), preferably at low temperature. The low temperature drying known to persons skilled in the relevant art is advantageous because, in contrast to high temperature drying, no harmful dioxins and furans are formed. Corresponding devices are previously known from the relevant prior art. Such a need exists in particular if fungus formation and spontaneous combustion shall be prevented and/or if the transport weight of the biochar/vegetable coal mixture loaded with nutrients shall be reduced. Low-temperature drying is preferably carried out at a DS content of at least 86% since fungus formation can only be prevented from this DS content on.

[0512] The produced biochars/vegetable coals/biocokes can be quenched individually or as a coal mixture H (RS 26) or as a coal conversion residue mixture I (RS 27) or loaded with nutrients, in particular with N-containing nutrients. The corresponding devices previously known from the relevant prior art only have to be arranged or switched accordingly (cf. claim 36).

[0513] If the aim of the downstream biochar additions 32/33/34 is to bind or immobilize the N-surplus in the (agriculturally used soil), the biochar masses E to G (RS 22 to 24) are not loaded with nutrients in method step 25. Quenching can then either be completely omitted (and thus the entire method step 25) or it is carried out with purified process water 17 or with fresh water.

[0514] In an advantageous embodiment of the invention (not shown in FIG. 1), the biochar masses E to G (RS 22 to 24) produced by means of quenching/loading 25 can be stored in a silo, container, bunker or similar device previously known from the relevant prior art, preferably sorted by type, until they are needed. This need can arise from downstream mixing 26, from downstream mixing 27, from downstream pelletization/briquetting 28, from downstream filling in BigBags 30 or from downstream loose distribution, e.g. by tank trucks via regional interim storage facilities 31.

[0515] In method step 26 (mixing to form a biochar mixture H), the up to three biochar masses E to G (RS 22 to 24) are mixed in any combination and with any proportions to form a biochar mixture H (RS 26). The biochar mixture 26 can also consist of only one of the three biochar masses E to G (RS 22 to 24) (cf. claim 10). The biochar masses E to G (RS 22 to 24) can, but do not have to, be quenched beforehand with process water. Likewise, the biochar masses E to G (RS 22 to 24) can have been, but do not have to be, loaded with nutrients before being mixed together. According to the invention, special designer biochar mixtures with different properties can be produced by such mixing. Thus, method step 26 makes it possible to adapt the subsequent biochar/vegetable coal application 33/34 to the area-specific demand for OPS, OSS, nutrient humus, permanent humus and/or organic carbon.

[0516] The shares of the up to three biochar masses E to G (RS 22 to 24) in the biochar mixture H (RS 26) can each be between 0% and 100% under the natural secondary condition that the sum of the shares does not exceed 100% (cf. claim 10).

[0517] Preferably the biochar mass E (RS 22) has a share of >1% of the total coal mixture H (RS 26), more preferably a share of >50% and in particular a share of >75%.

[0518] The biochar mass F (RS 23) preferably has a share of <99% of the total coal mixture H (RS 26), more preferably a share of <50%, in particular a share of <25% and at best a share of <10%.

[0519] Preferably, the coal mixture H (RS 26) is produced at least proportionally from straw-containing conversion residues (cf. claim 11).

[0520] A partial stream of the biochar mixture H (RS 26) produced in the process step Mixing 26 can be stored in a silo 29, container, bunker or similar device known from the relevant prior art until it is needed. This need can be based on filing in BigBags 30 (or other containers), loose distribution e.g. by tank trucks via regional interim storage facilities 31, pelleting/briquetting 28 (not shown in FIG. 1) or mixing 27 (not shown in FIG. 1). The share of the partial stream in the total biochar mixture H stream can be between 0% and 100%.

[0521] For the division into the BCM partial streams E to G, mixing 26, mixing 27 and the intermediate storage in silo 29, suitable devices previously known from the relevant prior art are used (cf. claim 36).

[0522] It is also possible that the mixing 26 of the up to three biochar masses E to G (RS 22 to 24) is only carried out on the occasion of application 32 (not shown in FIG. 1). For this purpose, the application and distribution devices (fertilizer spreaders, solid manure spreaders, slurry spreaders and similar distribution devices previously known from the relevant prior art) consist of up to three departments in which the type-pure biochar masses E to G (RS 22 to 24) are located. Appropriate sensors previously known from the relevant prior art, installed in front of the distribution devices in the direction of travel (e.g. on the tractor), measure the soil content, preferably the topsoil, of OPS, OSS, nutrient humus, permanent humus, organic carbon, nitrogen and/or other substances during application 32 and the biochar-mass-specific additions are then made according to the resulting need or in such a way that the set target value is reached. The same is possible by including the conversion residue D (RS 15). In this case, the up to three biochar masses E to G (RS 22 to 24) and the one conversion residue D (RS 15) are spread and applied from up to four departments.

[0523] In method step 27 (mixing to form a biochar conversion residue mixture I), the biochar mixture H (RS 26) and the conversion residue D (RS 15) are mixed in any proportions to form a biochar conversion residue mixture I (RS 27). The biochar conversion residue mixture I 27 can also consist of only one of the three biochar masses E to G (RS 22 to 24) or only of the biochar mixture H (RS 26) (see claim 10). The biochar conversion residue mixture 127 can, but does not have to, be quenched beforehand with process water 17. Likewise, the biochar conversion residue mixture I 27 or its components can have been, but do not have to be, loaded with nutrients before their production. According to the invention, special designer biochar mixtures with different properties can also be produced by this mixing 27. Thus, method step 27 allows an even better adaptation of the subsequent biochar/vegetable coal application 33/34 to the area-specific need for OPS, OSS, nutrient humus, permanent humus and/or organic carbon.

[0524] The shares of the up to three biochar masses E to G (RS 22 to 24) and/or the biochar mixture H (RS 26) in the biochar conversion residue mixture I (RS 27) can each be between 0% and 100% under the natural secondary condition that the sum of the shares does not exceed 100% (cf. claim 10).

[0525] Preferably the biochar conversion residue mixture I (RS 27) is produced at least proportionally from straw-containing conversion residues (cf. claim 11).

[0526] In the case of mixing 27, suitable devices previously known from the relevant prior art are used for this purpose (cf. claim 36).

[0527] It is also possible that the mixing 27 takes place only on the occasion of application 32 (not shown in FIG. 1). For this purpose, the spreading and distribution devices (fertilizer spreaders, solid manure spreaders, slurry spreaders and similar distribution devices previously known from the relevant prior art) consist of up to four departments in which the type-pure biochar masses E to G (RS 22 to 24) and the conversion residue D (RS 15) or the biochar mixture H (RS 26) and the conversion residue D (RS 15) are located. Appropriate sensors previously known from the relevant prior art and installed in front of the distribution devices in the direction of travel (e.g. on the tractors), measure the content of the soil, preferably the topsoil, of OPS, OSS, nutrient humus, permanent humus, organic carbon, nitrogen and/or other substances during application 32 and the biochar-mass-specific additions are then made according to the resulting need or in such a way that the set target values are reached.

[0528] In an advantageous embodiment of the example of the method and system according to the invention, shown in FIG. 1, the transport suitability of the produced biochar mixture H (RS 26) and/or of the biochar conversion residue mixture I (RS 27) is increased and/or its downstream application 32 is facilitated by method step 28 (pelletizing). The pelletization is carried out as it is previously known from practice and the relevant prior art, i.e. It can comprise a selection of the following sub-processes: drying, comminution, evaporation, pressing, cooling, conveying, warehousing, storage. Pelletizing 28 is carried out using appropriate devices and systems previously known from the relevant prior art.

[0529] The biochar/vegetable coal pellets or biocoke pellets produced by pelletizing 28 can be stored in a silo 29, container, bunker or similar device previously known from the relevant prior art until they are needed. This need can arise from the downstream filling in BigBags 30 (or other containers) or from downstream bulk distribution, e.g. by tank trucks via regional interim storage facilities 31. The interim storage of the biochar/vegetable coal pellets or biocoke pellets in silo 29 and all associated upstream and downstream sub-processes (first conveying, warehousing, storage, outplacement, second conveying, etc.) are carried out with suitable devices and systems previously known from the relevant prior art.

[0530] As shown in FIG. 1 by dashed lines leading from reference sign 27 to reference signs 30 and 31, it is also possible that the biochar-conversion residue mixture I (RS 27), which can consist of only the biochar mixture H (RS 26) or only one of the biochar masses E to G (RS 22 to 24) (see above), is not pelletized and is loosely filled in BigBags in subsequent method step 30 or loosely distributed in subsequent method step 31.

[0531] The biochar-conversion residue mixture I (RS 27), which may have been pelletized in method step 28 and can consist only of the biochar mixture H (RS 26) or only of one of the biochar masses E to G (RS 22 to 24) (see above), is preferably filled in BigBags in method step 30 but can also be filled in bags, containers and similar receptacles. It is also possible that the biochar-conversion residue mixture I (RS 27) is comminuted, preferably ground, prior to filling 30. This is advantageous if the biochar-conversion residue mixture I (RS 27) shall be spread together with other media, such as slurry, solid manure, fermentation residue, swill, fertilizer, lime, etc., on the (agricultural and/or forestry) areas. The degree of fineness of the comminution depends on the needs of the customer (farmer), it can comprise a particle length from 0.1 mm to 100 mm. Comminution and filling 30 are carried out using appropriate devices previously known from the prior art.

[0532] In method step 31, the possibly pelletized biochar-conversion residue mixture I (RS 27), which is filled in BigBags and can consist of only the biochar mixture H (RS 26) or only one of the biochar masses E to G (RS 22 to 24) (see above), is distributed to regional interim storage facilities, preferably by rail, ship and/or truck. The biochar-conversion residue mixture I (RS 27) filled in BigBags can also be delivered directly to the end consumers (farmers).

[0533] In an advantageous variant of the embodiment of the invention, shown in FIG. 1, the possibly pelletized biochar mixture H (RS 26) and/or the possibly pelletized biochar-conversion residue mixture I (RS 27) can also be distributed in bulk to the intermediate storage facilities and/or to the end consumers. For this purpose, suitable devices previously known from the relevant prior art are used, preferably tank trucks, designed for the transport of pellets or powdery products, such as cement or flour.

[0534] In method step 32, the loose or packaged biochar-conversion residue mixture I (RS 27), which can also consist only of the biochar mixture H (RS 26) or only of one of the biochar masses E to G (RS 22 to 24) (see above), is delivered directly from the biomass conversion plant or from one of the regional intermediate storage facilities to the agricultural or forestry enterprise and filled, with or without intermediate storage, in devices suitable for distributing the biochar-conversion residue mixture I (RS 27), the biochar mixture H (RS 26) and/or at least one of the biochar masses E to G (RS 22 to 24) on the areas into which these biochars/vegetable coals or mixtures shall be incorporated. These can be all devices previously known from the relevant prior art, preferably fertilizer spreaders or solid manure spreaders.

[0535] These biochars/vegetable coals can also be mixed with solid fertilizers, solid manure or other substances so that the fertilizer spreaders or sold manure spreaders load and spread appropriate mixtures. If these other substances are liquid, the application of the biochars/vegetable coals or mixtures can also be carried out with slurry spreaders or devices having equal functions. In the latter case, it can be advantageous to comminute the biochars/vegetable coals or mixtures beforehand to such a degree of fineness that the slurry distributors or devices having equal function do not clog.

[0536] The biochars/vegetable coals or mixtures are applied on agricultural and forestry land after loading the distribution devices as previously known from the relevant prior art or from practice.

[0537] In method step 33, the biochars/vegetable coals or corresponding mixtures spread on the agricultural or forestry land are worked into the sol, preferably into the topsoil. This incorporation is carried out as previously known from the relevant prior art and practice, preferably by ploughing, cultivating or harrowing, with devices previously known from the relevant prior art, preferably by means of tractor-drawn ploughs, cultivators, harrows or similar devices.

[0538] In an advantageous variant of the embodiment of the invention, shown in FIG. 1, the biochars/vegetable coals incorporated into the soil, preferably into the topsoil, or the corresponding mixtures (RS 22 to 24, 26 and 27) are at least partly produced from lignocellulose-containing input materials, preferably from straw. More preferably, these input materials were exposed to high reaction temperatures. The biochars/vegetable coals produced from conversion residues containing straw preferably have a pH of >7.0, more preferably >8.5 and in particular >10.0. Preferably, the biochar/vegetable coal/biocoke produced from conversion residues containing straw is applied to acidic soils (cf. claim 11).

[0539] In an advantageous embodiment of the method shown in FIG. 1, unloaded stabilized biochars/vegetable coals/biocokes are incorporated into overfertilized and/or sandy soils to reduce overfertilization and/or nitrogen wash. Preferably, 0.1 to 5000 t biochar/vegetable coal/biocoke dry mass are applied per hectare, more preferably 1 to 1000 t biochar/vegetable coal/biocoke dry mass, in particular 10 to 500 t biochar/vegetable coal/biocoke dry mass and at best 20 to 100 t biochar/vegetable coal/biocoke dry mass.

[0540] Preferably, at least 5 t biochar/vegetable coal/biocoke per hectare and 100 years are incorporated into the soil, more preferably at least 50 t biochar/vegetable coal/biocoke per hectare and 100 years and in particular at least 100 t biochar/vegetable coal/biocoke per hectare and 100 years (cf. claim 12).

[0541] In another advantageous embodiment of the method shown in FIG. 1, the biochar/vegetable coal mixtures produced are applied with a high proportion of pyrolysis coals prior to the cultivation of cereal crops, preferably with a proportion of >50% and in particular with a proportion of >75%.

[0542] Preferably, the biochar-conversion residue mixture I (RS 27) incorporated into the soil, preferably into the topsoil, is produced at least proportionally from straw-containing conversion residues (cf. claim 11).

[0543] In an advantageous embodiment of the method shown in FIG. 1, so much of the produced biochar/vegetable coal-conversion residue mixture I (RS 27) is worked into the soil, preferably into the topsoil, that the proportion of biomass growth, preferably the proportion of straw growth, which had to remain on the fields before the method was used to maintain the humus content of the soil, can be reduced, and thus increased access to the biomass growth, preferably to the straw growth, becomes possible.

[0544] Preferably, the increased access based on the total biomass growth or to the total straw growth is >0.1% points, more preferably >30% points, in particular >50% points and in the best case >75% points (cf. claim 12).

[0545] In an advantageous embodiment of the method and system, shown in FIG. 1, at least a portion of the atmospheric carbon-containing biochar mixture H (RS 26) is not incorporated into agricultural or forestry soil, but is sequestered/end stored in geological formations, in stagnant waters, in aquifers or in the ocean, in soils not or no longer used for agriculture or forestry, or in bogs, desert soils, permafrost soils (cf. claim 7).

[0546] In method step 34, the incorporated biochars/vegetable coals or the corresponding mixtures are activated. This consists of securing, preferably improving, soil quality. This is achieved by securing, preferably increasing, the OPS or OSS content, the nutrient humus content, the permanent humus content and/or the content of organic carbon. The ways in which this can be done are described above. In order to avoid repetitions, reference is made to the above explanations.

[0547] The biochar/vegetable coal mixtures provided by the method and system of FIG. 1 are preferably used to improve at least one of the yield limiting soil properties.

[0548] In the sense of the invention, however, the desired main effect of method steps 33/34 is that atmospheric carbon is permanently removed from the atmosphere of the earth as part of a fuel or heating medium or combustion material production process. This decarbonization prevents atmospheric carbon from reacting (again) with atmospheric oxygen to form CO.sub.2 or with hydrogen to form CH.sub.4 for millennia. Accordingly, the GHG emission value of the product of the method according to the invention, the energy carrier mix 9 (which can also consist only of the produced energy carrier 5 or the energy carrier mix 7), is improved relative to the GHG emission value of its fossil counterpart, preferably to such an extent that no GHG emissions are associated with the production, distribution and use of the energy carrier mix 9, more preferably to such an extent that after the production, distribution and use of the energy carrier mix 9 there are fewer greenhouse gases or GHG quantities in the atmosphere of the earth than before.

[0549] The embodiment of the invention described in FIG. 1 can be modified in many ways. For example, individual method steps can be omitted without changing the end products (EC-Mix 9 and/or the effect in the soil & in the atmosphere of the earth 34). In the following, some variants are listed with reference to the embodiment of FIG. 1 that describe circumstances in which individual method steps and accordingly the use of corresponding devices can be omitted. These embodiments are not all-encompassing; for a person skilled in the art who is aware of the invention, further circumstances are obvious, in the presence of which some individual method steps 1 to 3, 6 to 9, 11 to 19 and 22 to 34 can be obsolete or are not absolutely necessary.

[0550] Briquetting 19, for example, can also be carried out without previous disintegration 18. This is also the case with pelletizing 19 if the conversion residues A to C (RS 12 to 14) to be pelletized are small enough. Dehydration 16 is also not absolutely necessary, e.g. If, for example, an HTC shall be carried out in method steps 20/21 or if the conversion residues A to C (RS 12 to 14) have a DS content sufficient for efficient pyrolysis or torrefaction. Nutrient extraction 16 can be dispensed with, as can pelletizing 19, for example if carbonization processes are used in method steps 20/21 that function without pelletized input materials. If only one type of biochar mass E, F or G (RS 22 to 24) shall be produced and no conversion residue D (RS 15) is required, e.g. separation 11 is also superfluous. Pre-treatment 3 of the input materials 1/2 is also not absolutely necessary, e.g. If high conversion efficiencies shall not be achieved in the conversion 4 and/or the focus is more on ensuring that as large a proportion as possible of the atmospheric carbon contained in the at least one input material remains in conversion residue 10 in order to achieve as high a decarbonylation effect 34 as possible. Harvest and collection 2 can be omitted, for example, if at least one input material is produced anyway and therefore does not have to be harvested or collected. If the substance 1/2 to be used is given, e.g. method step 1 is superfluous. The mixtures 7 and/or 9 do not necessarily have to occur either, the desired GHG effect still occurs. Furthermore, under the circumstances described above, loading with nutrients 25 can be omitted. In the case of C-stabilization by carbonization of the conversion residues, for example, quenching 25 can be omitted if there is a corresponding alternative to cooling hot biochar/vegetable coal, e.g. cooing with air.

[0551] The mixtures 26 and 27 can be omitted if only one biochar mass E, F or G (RS 22 to 24) shall be produced. Filling in BigBags 30 can be omitted if e.g. filing in bags is carried out or if the produced biochar/vegetable coal mixture shall be distributed in bulk. Distribution to regional intermediate storage facilities 31 becomes obsolete if e.g. the end customer is supplied directly or if he collects the biochar/vegetable coal mixture himself at the biomass conversion plant. The loading of application devices and the application 32 as well as the incorporation into the field topsoil become superfluous if the biochar mixture H (RS 26) produced is sequestered elsewhere than in the soil used for agriculture or forestry.

[0552] The embodiment of the invention shown in FIG. 1, its sub-variants described above and the above-listed examples of shorter embodiments and other embodiments of the invention, which result from the entire above description, the claims and, where applicable, the reference signs, or which are obvious to a person skilled in the art after becoming aware of the invention, can also be extended in many ways. For example, it is possible to use devices and/or methods for the recuperation of process heat, for heat exchange and/or for heat recirculation, which can preferably include components that function according to the countercurrent principle (see claims 26 and 32). It is also possible, for example, top provide one or more conveyances and/or one or more intermediate storage between the individual method steps or between the individual devices by means of suitable devices previously known from the relevant prior art. These conveyances and/or intermediate storage can include the sub-methods of a first conveyance, warehousing, storage, taking out of storage and second conveyance. It is also possible, for example, that the biochar masses, biochar/vegetable coal mixtures, biochar conversion residue mixtures produced or the soil are provided with additives as known from the relevant prior art or from horticultural practice and/or plant cultivation before or after incorporation of the biochar (mixtures) produced. Furthermore, it is possible to put the produced biochar masses, biochar/vegetable coal mixtures, biochar conversion residue mixtures to uses previously known from the relevant prior art other than the incorporation into the soil 33. Such additional measures, as well as the devices used for them, are considered to be the usual current or future specialist knowledge of a competent person skilled in the art and shall also be protected.

[0553] FIG. 2 shows a schematic diagram of a further example of the method and system according to the invention for reasons of a clearer representation without the conversion residue D and its use indicated in FIG. 1. It goes without saying that the embodiment shown in FIG. 2 can also be carried out with conversion residue D and the use thereof, as shown in FIG. 1.

[0554] A first recuperation of atmospheric carbon dioxide (CO.sub.2 I) with reference sign 35 and a second recuperation of atmospheric carbon dioxide (CO.sub.2 II) with the reference sign 36 are added in FIG. 2. CO.sub.2-I (RS 35) can occur as a by-product or residue of conversion 4. The recuperation of CO.sub.2-I (RS 35) is carried out on the occasion of this (first) conversion 4 of the selected biomass 1/2 into a produced energy carrier 5. Such recuperation is e.g. possible in the production of bio-ethanol and in the processing of biogas into bio-methane. For the recuperation of CO.sub.2, suitable devices previously known from the relevant prior art are used, preferably pipelines with valves, especially pressurized gas pipelines.

[0555] The second recuperation of atmospheric carbon dioxide (CO.sub.2 II) takes place in method step 21 on the occasion of the chemical-physical stabilization of atmospheric carbon. CO.sub.2-II (RS 36) can occur as a by-product or as a residue of C-stabilization 21. Such CO.sub.2 recuperation 36 is e.g. possible in the carbonation of biomass, especially in the pyrolysis of biomass. The combustion of pyrolysis gas produces a flue gas with a high CO.sub.2 content.

[0556] The recuperated CO.sub.2 I (RS 35) and the recuperated CO.sub.2 II (RS 36) are combined, purified (RS 37), liquefied (RS 38) geologically sequestered (RS 39), used as a substitute for fossil CO.sub.2 (RS 40) or for the production of CO.sub.2-based energy carriers (RS 41), preferably for the production of syn-methane (cf. claim 13). These uses are advantageous because, due to the resulting decarbonization effects, the GHG emission values of the produced energy carrier 5 can be improved and consequently the admixture quantities of sustainable energy carrier 6 and/or fossil energy carrier 8 can be increased without affecting the GHG emission values of the energy carrier mixtures 7 and 9.

[0557] In order to implement this, devices previously known from the relevant prior art are used which are suitable for recuperating, liquefying, purifying, processing, storing, transporting (preferably in a liquid state of aggregation) atmospheric carbon doxide (CO.sub.2) produced in the method according to the invention, delivering it to industry, introducing it into geological formations, converting it into CO.sub.2-based fuel, heating medium or combustion material, performing a combination of these functions (cf. claim 37).

LIST OF REFERENCE SIGNS (KS)

[0558] 1 Selection of at least one biogenic input material containing atmospheric carbon or the selected input material itself [0559] 2 Harvesting/collection of the at least one biogenic input material (biomass) selected in 1 or the harvested/collected at least one input material itself [0560] 3 If necessary, pretreatment/disintegration of the at least one input material 2 or the pretreated input material itself [0561] 4 Single-stage or multi-stage conversion of the possibly pre-treated input material 3 into an energy carrier 5 containing atmospheric carbon 5 [0562] 5 Sustainable energy carrier resulting from 4, preferably used as transport fuel [0563] 6 Sustainably produced energy carrier from another conversion process with a higher GHG emission value than energy carrier 5, which is used in particular as a transport fuel [0564] 7 Mixing the energy carrier 5 with another sustainable energy carrier 6 to form an energy carrier mixture 7, wherein the energy carrier 5 is preferably bio-methane, the other sustainable energy carrier 6 is preferably syn-methane produced from wind power and atmospheric CO.sub.2 [0565] 8 Fossil energy carrier (fuel, heating medium or combustion material), preferably CNG or LNG [0566] 9 Mixing of the energy carrier mix 7 with a fossil energy carrier 8 to form an energy carrier mix 9, the mixing of which preferably takes place in such a way that, after the production, distribution and use of the energy carrier mix according to life cycle analysis or stoichiometric analysis, the amount of greenhouse gas in the atmosphere of the earth (measured in tons of CO.sub.2 equivalent) is the same or lower than after the production, distribution and use of an equal energy amount of the fossil counterpart of the energy carrier mixture, more preferably in such a way that, after the production, distribution and use of the energy carrier mix, a smaller amount of greenhouse gases is in the atmosphere of the earth than before, i.e. the energy carrier mix produced is GHG negative. [0567] 10 Recuperation of conversion residues (K residue) from 4 or the recuperated conversion residue itself [0568] 11 Distribution of the recuperated conversion residues CR [0569] 12 Conversion residue partial stream A [0570] 13 Conversion residue partial stream B [0571] 14 Conversion residue partial stream C [0572] 15 Conversion residue partial stream D [0573] 16 Dehydration by separation into a more solid and a more liquid phase, wherein the more liquid phase is used as process water, and/or extraction of organic nutrients [0574] 17 Process water, preferably containing nutrients [0575] 18 Disintegration [0576] 19 Pelletizing/briquetting [0577] 20 Generation of conditions which allow at least partial chemical-physical stabilization of the atmospheric carbon still contained in the conversion residue [0578] 21 Carrying out the chemical-physical stabilization of atmospheric carbon, preferably by carbonization, more preferably by pyrolysis or torrefaction [0579] 22 Resulting stabilized carbon, preferably contained in biochar/vegetable coal/biocoke (BC mass E) [0580] 23 Resulting partially stabilized carbon, preferably contained in biochar/vegetable coal/biocoke (BC mass F) [0581] 24 Resulting unstabilized carbon, preferably contained in biochar/vegetable coal/biocoke (BC mass G) [0582] 25 Loading the biochar/vegetable coal/biocoke masses E to G with organic nutrients, preferably with organic nutrients extracted from the conversion residue according to 16, more preferably by quenching the hot output of the pyrolysis/torrefaction devices with the more liquid phase obtained at 16 [0583] 26 Mixing of the biochar/vegetable coal/biocoke masses E to G loaded according to 25 to form a biochar/vegetable coal/biocoke mixture H or the biochar/vegetable coal/biocoke mixture H itself [0584] 27 Mixing the biochar/vegetable coal/biocoke mixture H mixed according to 26 with the conversion residue partial stream D to form a biochar/vegetable coal/biocoke conversion residue mixture I or the biochar/vegetable coal/biocoke conversion residue mixture I itself [0585] 28 Pelletizing, where appropriate, the biochar/vegetable coal/biocoke mixture H obtained according to 26, which can also be only a biochar/vegetable coal/biocoke mass E to G, and/or the biochar/vegetable coal/biocoke conversion residue mixture I obtained according to 27 [0586] 29 Possibly intermediate storage of the biochar/vegetable coal/biocoke masses E to G pelletized according to 28, of the biochar/vegetable coal/biocoke mixture H and/or the biochar/vegetable coal/biocoke conversion residue mixture I, preferably in silos 29 [0587] 30 Filling of loose and/or pelletized biochars/vegetable coals/biocokes, preferably in BigBags [0588] 31 Distribution of biochars/vegetable coals/biocokes packed in BigBags, if applicable, preferably to regional distribution points [0589] 32 Loading agricultural/forestry fertilizer, slurry and/or solid manure spreading devices, if necessary after further intermediate storage in the agricultural or forestry companies and spreading of the biochars/vegetable coals/biocokes E to G or with biochar/vegetable coals/biocoke mixtures H or with biochar/vegetable coal/biocoke conversion residue mixtures I preferably together with fertilizer, solid manure and/or slurry [0590] 33 Incorporation d into agricultural soil, preferably by ploughing, more preferably by ploughing into the topsoil [0591] 34 Effect of biochars/vegetable coals/biocokes or biochar/vegetable coal/biocoke mixtures or biochar/vegetable coal/biocoke conversion residue mixtures incorporated into the agricultural soil, which differs in the soil and atmosphere of the earth depending on the biochar/vegetable coal/biocoke type (E to q) incorporated into the soil [0592] 35 Recuperation of atmospheric CO.sub.2 I resulting from the single-stage or multi-stage conversion according to 4 of possibly pre-treated biomass 3 into a produced energy carrier 5 [0593] 36 Recuperation of atmospheric CO.sub.2 II, which is produced during (partial) stabilization 21 of atmospheric carbon [0594] 37 Purification of atmospheric CO.sub.2 recuperated according to 35 and/or 36, if necessary, [0595] 38 Liquefaction of atmospheric CO.sub.2 recuperated according to 35 and/or 36 [0596] 39 Sequestration of atmospheric CO.sub.2 in carbon sinks [0597] 40 Substitution of fossil CO.sub.2 with atmospheric CO.sub.2 [0598] 41 Manufacture of synthetic fuel, heating medium or combustion material from atmospheric CO.sub.2