WO2023275377A1 - Verfahren zum trocknen von vorzugsweise biogenen reststoffen und bioreaktor zur durchführung des verfahrens - Google Patents
Verfahren zum trocknen von vorzugsweise biogenen reststoffen und bioreaktor zur durchführung des verfahrens Download PDFInfo
- Publication number
- WO2023275377A1 WO2023275377A1 PCT/EP2022/068321 EP2022068321W WO2023275377A1 WO 2023275377 A1 WO2023275377 A1 WO 2023275377A1 EP 2022068321 W EP2022068321 W EP 2022068321W WO 2023275377 A1 WO2023275377 A1 WO 2023275377A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- bioreactor
- drying medium
- balls
- residues
- drying
- Prior art date
Links
- 238000001035 drying Methods 0.000 title claims abstract description 149
- 238000000034 method Methods 0.000 title claims abstract description 83
- 230000000035 biogenic effect Effects 0.000 title claims abstract description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 67
- 229910001868 water Inorganic materials 0.000 claims abstract description 49
- 238000011049 filling Methods 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 238000002156 mixing Methods 0.000 claims abstract description 29
- 238000000227 grinding Methods 0.000 claims abstract description 25
- 206010039509 Scab Diseases 0.000 claims abstract description 22
- 230000008569 process Effects 0.000 claims description 53
- 230000002093 peripheral effect Effects 0.000 claims description 20
- 239000002023 wood Substances 0.000 claims description 8
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 150000002505 iron Chemical class 0.000 claims description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 4
- 235000010099 Fagus sylvatica Nutrition 0.000 claims description 4
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 4
- 239000004571 lime Substances 0.000 claims description 4
- 238000005299 abrasion Methods 0.000 claims description 3
- 238000012216 screening Methods 0.000 claims description 3
- 240000000731 Fagus sylvatica Species 0.000 claims 1
- 238000010521 absorption reaction Methods 0.000 claims 1
- 239000000843 powder Substances 0.000 description 72
- 239000003570 air Substances 0.000 description 59
- 239000002245 particle Substances 0.000 description 35
- 230000005291 magnetic effect Effects 0.000 description 24
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 description 22
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 21
- 229910000398 iron phosphate Inorganic materials 0.000 description 21
- 229910052698 phosphorus Inorganic materials 0.000 description 21
- 239000011574 phosphorus Substances 0.000 description 21
- 239000010408 film Substances 0.000 description 20
- 239000007787 solid Substances 0.000 description 13
- 239000007789 gas Substances 0.000 description 11
- 239000012071 phase Substances 0.000 description 11
- 239000000126 substance Substances 0.000 description 11
- 238000003860 storage Methods 0.000 description 10
- 239000000463 material Substances 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 229910019142 PO4 Inorganic materials 0.000 description 8
- 150000001875 compounds Chemical class 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- 235000015097 nutrients Nutrition 0.000 description 8
- 235000021317 phosphate Nutrition 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- 238000009835 boiling Methods 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 230000008020 evaporation Effects 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000010802 sludge Substances 0.000 description 6
- 239000002274 desiccant Substances 0.000 description 5
- 210000003608 fece Anatomy 0.000 description 5
- 238000000855 fermentation Methods 0.000 description 5
- 230000004151 fermentation Effects 0.000 description 5
- 239000010871 livestock manure Substances 0.000 description 5
- 150000002739 metals Chemical class 0.000 description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 5
- 239000010452 phosphate Substances 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- 230000007704 transition Effects 0.000 description 5
- 238000009834 vaporization Methods 0.000 description 5
- 230000008016 vaporization Effects 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 241000196324 Embryophyta Species 0.000 description 4
- 239000003337 fertilizer Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000011159 matrix material Substances 0.000 description 4
- 150000002736 metal compounds Chemical class 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 241001070947 Fagus Species 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 3
- 238000005273 aeration Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000002803 fossil fuel Substances 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000007885 magnetic separation Methods 0.000 description 3
- 239000006148 magnetic separator Substances 0.000 description 3
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 239000007858 starting material Substances 0.000 description 3
- 239000010409 thin film Substances 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 241000237858 Gastropoda Species 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000012080 ambient air Substances 0.000 description 2
- 239000011324 bead Substances 0.000 description 2
- 239000013590 bulk material Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 235000013339 cereals Nutrition 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000001419 dependent effect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000035622 drinking Effects 0.000 description 2
- 235000013312 flour Nutrition 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- 239000008241 heterogeneous mixture Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 230000005298 paramagnetic effect Effects 0.000 description 2
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 2
- 238000004886 process control Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000013535 sea water Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 229920001587 Wood-plastic composite Polymers 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 239000007900 aqueous suspension Substances 0.000 description 1
- 230000004323 axial length Effects 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 230000004069 differentiation Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000001747 exhibiting effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000005429 filling process Methods 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 239000006249 magnetic particle Substances 0.000 description 1
- 239000006247 magnetic powder Substances 0.000 description 1
- 229910001463 metal phosphate Inorganic materials 0.000 description 1
- 238000002663 nebulization Methods 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 235000019645 odor Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000000275 quality assurance Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000011012 sanitization Methods 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 239000011155 wood-plastic composite Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F33/00—Other mixers; Mixing plants; Combinations of mixers
- B01F33/25—Mixers with loose mixing elements, e.g. loose balls in a receptacle
- B01F33/251—Mixers with loose mixing elements, e.g. loose balls in a receptacle using balls as loose mixing element
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B11/00—Machines or apparatus for drying solid materials or objects with movement which is non-progressive
- F26B11/12—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in stationary drums or other mainly-closed receptacles with moving stirring devices
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B11/00—Machines or apparatus for drying solid materials or objects with movement which is non-progressive
- F26B11/12—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in stationary drums or other mainly-closed receptacles with moving stirring devices
- F26B11/14—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in stationary drums or other mainly-closed receptacles with moving stirring devices the stirring device moving in a horizontal or slightly-inclined plane
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B3/00—Drying solid materials or objects by processes involving the application of heat
- F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
- F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B3/00—Drying solid materials or objects by processes involving the application of heat
- F26B3/18—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact
- F26B3/20—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact the heat source being a heated surface, e.g. a moving belt or conveyor
- F26B3/205—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact the heat source being a heated surface, e.g. a moving belt or conveyor the materials to be dried covering or being mixed with heated inert particles which may be recycled
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B5/00—Drying solid materials or objects by processes not involving the application of heat
- F26B5/16—Drying solid materials or objects by processes not involving the application of heat by contact with sorbent bodies, e.g. absorbent mould; by admixture with sorbent materials
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B2200/00—Drying processes and machines for solid materials characterised by the specific requirements of the drying good
- F26B2200/12—Manure
Definitions
- the invention relates to a method for drying preferably biogenic residues with the supply of a drying medium.
- the invention also relates to a bioreactor for carrying out the method.
- Biogenic residues offer several potentials, in particular nutrients, energy, phosphorus and metals, which are often underused by the current process chains. Biogenic residues are often only disposed of and not recycled.
- biogenic residues are often in a chemically unstable and aqueous form and are not worth transporting over long distances. Examples include liquid manure and fermentation residues.
- the energetic potential of biogenic residues is the energy chemically bound in the complex organic molecules, which can be used as a biomass fuel to directly replace fossil fuels.
- Metals can be contained in the solids in different concentrations and combinations. Some metals are rare elements found only in small concentrations in the earth's crust. This includes, for example, cobalt, which is required in battery production for electromobility, so that the raw material is currently in high demand.
- the invention is based on the object of specifying a method with which, in particular, biogenic residues are processed in order to existing potential, especially nutrients, energy, phosphorus, metals and water as recyclable materials. Furthermore, the invention is based on the object of creating a bioreactor with which the method can be carried out.
- the process is characterized by the following steps: a) filling biogenic residues with a liquid portion into a bioreactor, b) drying the residues to a dry mass, c) grinding the dry mass, d) removing the dry mass.
- the dry mass can be further dried.
- the method has the following steps: a) Filling the residues having a liquid portion into a bioreactor filled with (preferably dry) balls and having a mixer and mixing the balls and the residues by operating the mixer at least intermittently during the filling and /or after filling, so that films of the residues form on the surfaces of the spheres, b) drying the films of residues to form crusts of dry matter with a residual water content on the surfaces of the spheres by feeding a drying medium into the bioreactor, which Flows around balls, with at least part-time operation of the mixer, c) grinding and further drying of the dry matter by at least part-time operation of the mixer with abrasion of powdery dry matter from the balls, d) removal of the powdery dry matter from the bioreactor.
- the result of the process is a very dry and very finely divided powdery dry mass (hereinafter also simply referred to as powder), which can be used in a variety of ways depending on the starting material (the residue).
- the powder can be used in particular as a substitute fuel for fossil fuels, in particular wherever a combustion process using fossil fuels, in particular coal, is currently taking place.
- An example represents the cement industry when burning clinker. In this way, fossil CC> 2 emissions can be effectively reduced.
- the dry mass can be used as a nutrient-rich fertilizer in agriculture in the form of dry flour, in particular by mixing chemically unstable manure or fermentation residues with particularly dry biogenic residues, whereby the nutrients of the residue are used.
- the process allows the phosphorus contained in the residue to be recovered and, in particular, also to be used as fertilizer.
- metals can be extracted from the residues in order to be used as raw materials in the production processes of goods.
- the water discharged from the reactor with the drying medium by the process can be used later by being treated as industrial or drinking water.
- seawater two recyclable materials are produced simultaneously: salt as dry matter and water by separating the water from the drying medium with subsequent processing into drinking or process water.
- residue is understood broadly within the scope of the invention and includes in particular, but not exclusively, biogenic residues.
- Biogenic residues are organic waste and waste water, agricultural and forestry by-products and biogenic production residues.
- residue for the description of the starting materials of this process includes all heterogeneous mixtures of substances with organic components. These are i.a. Sewage sludge (primary sludge, secondary sludge, tertiary sludge, digested sludge) and also liquid manure, fermentation residues, pond or river sludge, seawater and algae as well as other residues from marine plants and animals, as well as other organic mixtures of substances, secondary raw materials and industrial sludge.
- the dry mass can be further dried.
- the process comprises two stages, the first stage also being referred to as the “wet” stage and the second stage being referred to as the “dry” stage referred to as.
- the films of residues are essentially dried with the formation of crusts on the surfaces of the spheres with at least intermittent operation of the mixer, which also causes the powder to be separated from the spheres.
- the grinding and further drying of the powdery dry matter already separated from the spheres is carried out by operating the mixer through the grinding action of the spheres and discharging the powdery dry matter from the bioreactor.
- the "dry” stage which includes further drying and grinding, can be carried out as an independent process and in addition to the first stage.
- the drying medium is a drying fluid, in particular a gaseous fluid.
- warm, unsaturated air and/or unsaturated, superheated steam are preferably used as gaseous drying fluids.
- the application of the principle of steam drying using superheated water vapor also leads to a significant increase in the efficiency of heat transfer and thus time savings compared to using warm, unsaturated air as a drying medium.
- the principle of steam drying using superheated steam at atmospheric pressure is known per se.
- the drying process is accompanied by the evaporation of liquid, especially water (moisture).
- the evaporation of liquids is defined as a phase change from the liquid to the gaseous phase and thus the conversion of the liquid into vapor.
- steam is a real gas that can be discharged from the reactor space, which in the present case takes place through the drying medium.
- evaporation is a generic term that very generally describes the phase transition from the liquid to the gas phase and thus includes evaporation below the boiling point and boiling above the boiling point of a liquid.
- Water vapor can be part of a gas mixture.
- the water vapor in the atmosphere is part of the gas mixture of humid air.
- Humid air is a mixture of dry air and water. Compared to other mixtures of ideal gases, humid air has the special feature that water vapor cannot be mixed with dry air in any desired quantity.
- the amount of water vapor that can be contained in the air is such that the partial pressure of the water vapor (partial pressure) has reached the saturation pressure. If the partial pressure of water vapor is less than the saturation pressure, then the air is unsaturated. Steam with a temperature higher than the saturation temperature is unsaturated, superheated steam. On the one hand, water vapor in the unsaturated moist air below the boiling point is superheated vapor. On the other hand, a vapor can appear completely isolated and fill a space alone, especially if the vapor is kept above the boiling temperature.
- the energy can be introduced by convection (in the present inventive case using the drying medium) and/or conduction (via hot contact surfaces, e.g. heated outer walls of the bioreactor according to the invention) and/or by radiant heat (e.g. through transparent outer walls of one described later). bioreactor according to the invention).
- the supplied biogenic residues can preferably be heated before the supply (maximum up to the boiling point).
- the intensity and combination of the various heat transfer processes depend on the material properties of the biogenic residue to be dried and the desired drying result, which also includes disinfection/sanitization.
- heat transfer by convection is used with the aid of the drying medium.
- thermo and the pressure can be additionally varied for optimal process control and product quality, since these parameters directly influence the drying process.
- the boiling temperature is a dependent function of the set pressure level. Temperatures above 0° C. up to 250° C. and positive (overpressure) or negative (negative pressure) pressure differences of 0-4 bar in relation to atmospheric pressure are preferably set.
- the spheres can be made of any material as long as it has sufficient water absorbency in terms of hygroscopicity and/or capillarity and strength having.
- the balls are preferably made of wood and in particular beech wood.
- the spheres can be made of another material that has properties similar to wood, particularly in terms of moisture management and strength. For example, wood-plastic composites come into question.
- the diameter of the balls is preferably between 5 mm and 50 mm, particularly preferably between 15 mm and 30 mm.
- these can be dried before filling or feeding in the residual material. This can be done in particular by feeding the drying medium, in particular warm, unsaturated air and/or unsaturated, superheated steam, into the reactor.
- a mixing process can be carried out while the residues are being filled in. At least one mixing process is preferably carried out after filling. As a result, the residues are completely mixed with the balls at least once.
- the mixing process or processes continue until uniform thin films of the residues have formed on the surfaces of the balls.
- liquid can also be applied to the surfaces of the balls when filling the residues.
- the liquid can be introduced in particular by spraying in the liquid in the form of a spray mist.
- the liquid can be water or another (biogenic) residue with a higher moisture content. This means that drier and wetter residues that are fed in at the same time can be fixed to the surfaces of the balls as thin biofilms.
- liquid manure or fermentation residues are used as further (biogenic) residues with higher moisture contents.
- a nutrient-rich fertilizer mixture can be produced as dry flour and thus as dry stabilizer using the process presented here.
- Additional liquid is preferably introduced when the moisture content of the residue used falls below a lower threshold.
- the liquid supplied can be enriched with an iron salt in order to precipitate free phosphates in the residue as iron phosphate.
- the liquid can contain lime (calcium carbonate CaCCh) and can be added, for example, in the form of milk of lime and evenly distributed on the spherical surfaces.
- lime calcium carbonate CaCCh
- lime can also be fed into the bioreactor as a solid, in particular in the form of a free-flowing powder.
- the addition of lime increases the pH value of the biofilms that form on the spherical surfaces, which enables a targeted reduction in the temperature level, which is necessary for the phase transition of nitrogen, which is mostly available in the form of ammonium in the biogenic residues, from the liquid to the gaseous phase is required.
- gaseous discharge of ammonia can be specifically influenced with the help of the drying medium.
- the gaseous nitrogen that is discharged as a result can then be processed further and thus separated as a nutrient.
- This can preferably be done with an acid scrubber using sulfuric acid (H2SO4) so that ammonium sulphate solution can be produced.
- the warm, unsaturated air is preferably introduced into the bioreactor at a temperature of up to 85°C.
- the introduced air then flows around the spheres, with the films adhering to the sphere surfaces releasing moisture into the air.
- the saturated air is discharged from the bioreactor again.
- the water contained in the saturated air can be used for other purposes.
- the unsaturated, superheated steam is introduced into the bioreactor in particular at a temperature of 110° C. to 300° C., preferably 110° C. to 250° C.
- the set process parameters can be varied with regard to pressure and temperature, taking into account the limit values for the gas phase, which are derived from the vapor pressure curve.
- the water vapor is preferably introduced into the bioreactor at atmospheric pressure.
- the superheated steam then flows around the balls.
- the residues absorb the heat convectively.
- the films adhering to the surfaces of the spheres, which have a liquid content evaporate moisture, which the superheated steam absorbs as a real gas.
- the moisture removed from the biogenic residues thus becomes excess steam, which can be extracted again from the Bioreactor is derived.
- the water contained in the discharged excess steam can be used for other purposes.
- crusts form on the surfaces of the balls, which consist of dry matter with a residual water content. Due to the mixing processes, the crusts are finely ground (rubbed off) from the surfaces of the spheres and will settle as a powder (powdery dry matter) with a residual water content at the bottom of the bioreactor.
- the drying medium is preferably supplied via a plurality of drying medium inlets arranged at different heights of the bioreactor, in particular a drying medium inlet arranged in the lower third of the bioreactor, a drying medium inlet arranged in the middle filling level area, a drying medium inlet arranged above a maximum filling level and a drying medium inlet arranged in the bottom area .
- the drying medium supply in the lower area of the bioreactor in particular from the drying medium inlet arranged in the lower third of the bioreactor and the drying medium inlet arranged in the bottom area, can be reduced or switched off. The result of this is that the drying medium no longer flows through the powdery dry mass accumulating in the floor area. This prevents the highly flammable powder from being whirled up and discharged with the exhaust air or excess steam. This measure therefore serves not only to retain the powder in the reactor, but also to protect against explosion.
- the powder at the bottom of the bioreactor is preferably dried indirectly, with the drying medium not flowing through it directly (“aeration”).
- the indirect drying can take place via the surfaces of the balls, in particular by sorption and additional capillary suction forces, which are located in the powder mixture in the bottom area of the bioreactor and are preferably drier than the powder surrounding them.
- the drying medium can flow around the balls located above the powder during grinding and be dried in the process.
- the drying medium is supplied via the drying medium inlet arranged in the central filling level area and the drying medium inlet arranged above the maximum filling level drying medium inlet, while there is no drying medium supply from the other drying medium inlets.
- the reduction in size of the individual particles in the form of agglomerates is determined and limited, among other things, by the water molecules, which act as adhesive liquid bridges between the particles. By removing the water molecules, the particles can be increasingly isolated down to the single-digit pm range.
- Indirect drying via the surfaces/boundaries of the spheres also preferably allows powder to be dried cold, in that fully dried spheres are mixed into a powder bed, with the temperatures of the spheres and the powder not exhibiting any large temperature differences.
- a drying result with indirect drying, a complete drying of powder with a dry residue content of up to 98% can be achieved.
- the spheres and powder are preferably mixed intermittently.
- the mixing processes grind the powder through the friction on the surfaces of the balls.
- the residence time of the biogenic residues in the bioreactor can be set for a predetermined period of time, which is based on the respective legally valid specifications for hygienization.
- a bioreactor set up for carrying out the method according to the invention has the following features: a housing with at least one base and a preferably closed peripheral wall, a mixer which is preferably mounted rotatably about a vertical axis on the base and is arranged within the housing at least a drying medium inlet arranged in the central region or in the middle in the peripheral wall of the housing, based on a height of the housing or on a maximum filling level (Hiu ax ) of the housing, at least one drying medium outlet, a filling of the bioreactor from a large number of balls, with an initial fill level (Hstart), at least one feed line for residues, and at least one discharge device for removing the dried residues.
- Hiu ax maximum filling level
- Another desiccant inlet can be located in the bottom or in the peripheral wall.
- a cumulative arrangement in the base and in the peripheral wall can also be provided.
- a plurality of drying medium inlets can be provided in the peripheral wall and also in the base in order to ensure an adequate supply of drying medium.
- the bioreactor can comprise a plurality of drying medium inlets, in particular a drying medium inlet arranged in the lower third of the bioreactor in the peripheral wall, the drying medium inlet arranged in the middle filling level area in the peripheral wall, a drying medium inlet arranged above the maximum filling level in the peripheral wall or a cover and/or one drying medium inlet arranged in the floor.
- the drying medium can be fed in and distributed in a punctiform manner and/or via distributor plates which each have a large number of holes and extend over at least part of the reactor cross section. This means that drying medium can be supplied and distributed over defined areas.
- the housing can preferably be covered by a cover.
- the residues are preferably supplied and the drying medium is removed through the cover, in which corresponding openings are provided.
- the drying medium can be discharged and the residues can be fed in through the lateral peripheral wall above the maximum fill level by providing appropriate openings.
- the residues can also alternatively be fed into the lateral peripheral wall below the surface of the maximum filling level, preferably with a screw. In itself, it is irrelevant from where or at which point the biogenic residues are fed into the bioreactor.
- the mixer is preferably a vertical screw.
- the vertical screw can preferably be conical or cylindrical.
- On the snail coils or Screw blades (segmented screw) can preferably also have at least one knife and a scraper bar attached to the start of the screw.
- the mixer is preferably mounted on the bottom of the housing.
- the housing is preferably of cylindrical or conical design.
- the housing is preferably thermally insulated in order to be able to keep the temperature in the bioreactor constant during the drying process.
- the exhaust air or excess steam can be removed from a closed bioreactor by internal pressure or by applying a negative pressure.
- the applied temperatures can be varied by varying the applied pressures. In the case of a negative pressure, the temperature can be lowered and in the case of an overpressure, the temperature can be increased.
- the construction of the bioreactor is to be designed with a lid according to the selected pressure conditions.
- the aim of the first process step is the even distribution of the supplied (biogenic) residues on the surfaces of the spheres in the form of thin films with a layer thickness of preferably a few millimeters.
- the residues are preferably fed into the bioreactor above the bead bed.
- the balls are preferably made of wood, in particular beech wood. Alternatively, other moisture-regulating substances that have sufficient strength on the surfaces can also be used.
- the diameter of the spheres can preferably be between 5 and 50 mm. For example, around 73,000 balls with an average diameter of 25 mm are used per cubic meter of volume used in the bioreactor. The sum of the spherical surfaces per cubic meter is 144 m 2 (square meters).
- spherical bodies are preferably used for carrying out the method.
- preferably round or oval shaped bodies can also be used.
- the residues are preferably fed in while the mixer is operated at least intermittently in order to bring about a mixing process of the balls and residues.
- the mixing process should preferably last several minutes so that an even film can form on all balls.
- the mixing process takes place in the bioreactor, preferably by means of a vertical screw.
- the supplied residues can have different material properties and particle sizes.
- a supplied mixture can consist of liquid, wet, moist, sticky, solid, crumbly and powdery fractions at the same time.
- the size of the solid particles supplied can also vary in a range from 1 ⁇ m in a suspension to several centimeters as solid lumps.
- water is preferably filled into the bioreactor in order to pre-slurry or slurry the dry fractions. This can preferably be done by a spray mist above the balls and during the mixing process.
- a further special feature of the supplied residues can be the phosphorus they contain.
- the availability in the form of iron phosphate or another paramagnetic metal phosphate in the residues is desirable, which allows magnetic separation of substances, in particular by means of a magnetic effective separator (absorber).
- the phosphate contained in the (biogenic) residue is present in the form of a non-magnetic metal salt or as dissolved phosphate
- water that has been enriched with a suitable iron salt can be fed to the bioreactor.
- the supply is preferably in the form of a spray above the balls during the mixing process during the supply of residues.
- the supplied aqueous iron salt solution is evenly mixed into the films by the mixing process and then, in the presence of phosphate dissolved in the aqueous films, leads to a precipitation of phosphate as iron phosphate within a few minutes.
- One form of stabilization is the conversion to the state of a dry stabilizer. Due to the lack of water, the transport of nutrients is prevented for the mostly heterotrophic bacteria, which very quickly begin to break down the organic components, and thus the biological breakdown of the easily degradable organic substances is effectively stopped.
- the balls are preferably dried before filling.
- water is drawn from the wet film via capillary attraction forces across the sphere interfaces from the outside in into the drier cell cavities of the spheres as free water.
- the film is dried by removing moisture from the inside and is stabilized by the dry rigidity that accompanies it.
- the hygroscopic property of the balls allows the humidity to be adapted to the prevailing external conditions.
- the associated ability to store moisture enables very aqueous suspensions to be fed into the bioreactor, the water content of which can be absorbed up to the saturation limit of the balls.
- the biogenic residues which are present in the form of wet films on the balls, are dried by supplying a drying medium, preferably at a temperature above room temperature to 85 °C using warm, unsaturated air as the drying medium and preferably at a temperature above 110 °C C when using unsaturated, superheated steam as a drying medium.
- the drying medium is preferably supplied at a number of points which are arranged at different heights of the bioreactor.
- the drying medium is preferably supplied from the bottom of the reactor, from its Circumferential wall, specifically in the area of the balls at the height of the powder accumulation and in the area of the balls above the powder accumulation and above the ball bed.
- the aqueous surfaces of the films dry in this phase primarily by releasing water as water vapor into the unsaturated warm air flowing around them, and water is thus discharged from the bioreactor as water vapor via the more saturated exhaust air.
- the aqueous surfaces of the films dry in this phase mainly by releasing water as water vapor in the form of a real gas into the unsaturated, superheated water vapor flowing around them, and water is thus discharged from the bioreactor as excess vapor.
- the preferred mechanical intermixing of the spheres leads to an increase in the wet surfaces, in that the wet films transfer moisture to drier films and, after mixing, are again formed into homogeneous wet biofilms.
- the dry crusts should preferably increase the diameter of the balls by 5% up to 10%. This increases the volume used in the reactor by up to 33%.
- the filling density of the spherical matrix is around 60%, so that a free volume (air volume when using warm, unsaturated air as drying medium and steam volume when using unsaturated, superheated steam as drying medium) of around 40% remains.
- the mixing processes lead to the trickling substances being ground into a micro-fine powder.
- the particle size is less than 100 ⁇ m and preferably less than 60 ⁇ m. Individual particles are ground down to the single-digit pm range.
- the dry mass is further dried.
- the type of drying changes.
- the powder is no longer dried directly via the drying medium, but indirectly via the capillary suction forces and sorption on the dry boundary surfaces of the spheres.
- the water in the powder is therefore transported via the boundary surfaces of the spheres by sorption and capillary forces of attraction from the outside inwards into the cell cavities of the spheres and is bound there.
- the part of the balls not covered by powder which is above the layer of powder deposited on the ground, continues to be dried by the drying medium, when using warm, unsaturated air as the drying medium by the warm and unsaturated air flow, and when using unsaturated, superheated steam as the drying medium dried by the superheated and unsaturated steam flow.
- a subsequent mixing process mixes very dry balls from the upper area into the powder in the lower area of the bioreactor.
- the balls that are in the powder and that have previously been enriched with water from the powder are mixed from the powder into the upper part of the bioreactor and thus above the powder layer into the balls located there.
- the final dry residue content of the powder should preferably be between 90% and 98% by weight, i.e. have a moisture content of at most 10% by weight and up to 2% by weight.
- the grinding process is preferably carried out until the balls are essentially free of dry matter, i.e. the crusts are largely removed.
- the powder can preferably be carried out of the reactor pneumatically with the drying medium, in particular by suction air or negative pressure with the aid of cyclones. Heavier contaminants can be easily separated in the flow of the drying medium, especially in the air flow, using the air separation process.
- the powder can be discharged via a discharge device comprising lateral openings or openings in the bottom area of the reactor.
- a sieve device in particular a perforated plate or a grid or bars, can preferably be arranged in front of the openings in order to hold back at least the balls and optionally coarser components of the dry matter.
- a device for selectively opening and closing the discharge device can also be arranged in front of the screening device on the inside of the housing.
- the discharged dry matter can now be subjected to further quality assurance.
- This preferably includes the process for separating phosphorus, in particular in the form of iron phosphate.
- externally supplied dry matter can also be integrated into the phosphorus separation process.
- Iron phosphate is paramagnetic and is present in particular in particle sizes from 5 ⁇ m to 50 ⁇ m.
- the dry mass In order to enable separation from the hygroscopic bulk material in powder form, the dry mass must preferably be comminuted to a maximum size of 100 ⁇ m with a simultaneously high dry residue content of more than 90% up to 98%.
- These two parameters are essential to achieve free-flowing pourability and to avoid clumping in the powder.
- clumping has a direct impact on the degree of purity of the separated iron phosphate particles, since foreign matter adheres with increasing clumping.
- the grinding of the dry mass for the purpose of separating off the phosphate can be carried out in a mill or generally in a comminution unit.
- the device should enable the particles to be reduced to a grain size of ⁇ 100 ⁇ m.
- a purely mechanical comminution of the particles is limited by the residual moisture in the dry matter.
- the comminution can be carried out to the be inhibited in the single-digit pm range.
- a further preferred alternative process control is then the supply or return of the externally supplied or discharged and preferably comminuted dry matter in the process phase (c) grinding and drying the dry matter until the necessary dry residue content is reached, which means that comminution is preferably in the single-digit ⁇ m range allows.
- drying and grinding of externally supplied or discharged and preferably pulverulent dry mass can preferably take place or be continued in a second, separate mixer as an independent process.
- magnetic metal compounds in particular iron phosphate
- a magnetic separator in that the iron phosphate particles are attracted by the magnetic field and settle directly on the magnet or on a plate in front of it.
- the by-product iron phosphate is separated from the main product of the powdered dry matter.
- the magnetic separation can be done in different ways.
- a baffle plate in the drop section can lead to nebulization of the dry mass, from which the fine iron phosphate particles are then magnetically separated.
- a tubular magnet can be used for free-fall applications, as is also used in the pharmaceutical industry for separating weakly magnetized particles.
- a drum magnet, an overbelt magnet or other magnet systems can be used for separation.
- the magnet is advantageously an electromagnet, which particularly preferably magnetizes the housing wall of a storage container. With such an embodiment, it may already be sufficient to fill the powder from above into the storage container in free fall, so that it swirls on the baffle plate. The iron phosphate particles then settle on the housing wall.
- FIG. 0 shows the schematic representation of an unfilled bioreactor according to an embodiment of the invention
- FIG. 1 shows the schematic representation of the bioreactor from FIG
- FIG. 2 shows the schematic representation of the bioreactor from FIG .
- FIG. 3 shows the schematic representation of the bioreactor from FIG.
- FIG. 4 shows the schematic representation of the bioreactor from FIG.
- FIG. 5 shows a schematic representation of a plant for separating a magnetic, phosphorus-containing compound, in particular iron phosphate, in a state with excited magnets;
- FIG. 6 shows a schematic representation of the system from FIG. 5 with deactivated magnets.
- the bioreactor 0 is a thermal dryer which, in the exemplary embodiment shown in FIG. 0, consists of a housing 1 which is open at the top and which is conical and essentially consists of a closed peripheral wall 1.2 and a base 1.1.
- the schematic representation does not show that the housing 1 of the bioreactor 0 can be thermally insulated in order to be able to keep the temperature inside the bioreactor 0 as constant as possible.
- a preferably conical screw 2 is rotatably driven about the vertical axis A.
- the screw 2 has at least one turn 2.1.
- the snail 2 is shown shortened here. Their axial length preferably extends up to the maximum fill level H max in order to enable the quickest and most rapid mixing possible.
- the drying medium which is preferably ambient air and/or unsaturated, superheated steam, which is fed into the interior of the bioreactor 0, which allows the drying of the biogenic Residues 4 is used.
- the supply line 6 is in the lower third, the supply line 6.1 in the middle and one further supply line 6.2 above the bead bed (see FIG. 1).
- the supply line 6.3 is located in the floor 1.1.
- the ambient air can preferably be heated to a temperature in the range from 20 °C to 85 °C.
- unsaturated, superheated steam can preferably be heated to a temperature in the range from 110 °C to 250 °C.
- balls here wooden balls 3, which are preferably made of beech wood with a diameter of preferably 5-50 mm as bulk material, are inserted via the upper opening shown in Figure 0 into the bioreactor 0 to filled to a level of Hstan.
- the bioreactor 0 can be closed with a cover 1.3, which is shown in FIG.
- the structure of the bioreactor 0 shown in FIG. 1 corresponds to that of the bioreactor 0 according to FIG.
- the supply lines for biogenic residues 4 and water 5 and the discharge line for the exiting drying medium 7 lead through the cover 1.3.
- the wooden balls 3 are preferably dried in order to create a high potential in the wooden balls 3 for absorbing moisture.
- the drying medium is preferably supplied via all supply lines 6, 6.1, 6.2 and 6.3 in order to introduce heat into the bioreactor 0 for drying.
- the drying medium is warm, unsaturated air and/or unsaturated, superheated steam.
- the supply of warm air and/or steam via the feed line 6.3 serves as a leakage medium (leakage air and/or leakage steam) for discharging the saturated air and/or the excess steam from the lower part of the bioreactor 0, which and/or which previously flows through the spherical matrix Has.
- the exhaust air and/or the steam is discharged via the discharge line 7 in the cover 1.3.
- a slight negative pressure is preferably set in the bioreactor 0 by the air streams and/or steam streams.
- the aeration and deaeration and/or the steam supply and steam removal preferably take place continuously.
- the specific design of the air supply and/or the steam supply with regard to the duration, the volume flow and the temperature with regard to the individual air supply lines and/or steam supply lines 6, 6.1, 6.2 and 6.3 is variable with the aim of obtaining optimal conditions for the drying process.
- the vertically arranged screw 2 is put into operation in rotation and, preferably at the same time, the biogenic residues 4 are fed in via the feed line in the cover 1.3.
- the mixing process leads to the biogenic residues 4 being mixed with the wooden balls 3 and preferably lasts several minutes.
- the mixing process ends with largely homogeneously formed biofilms on the surfaces of the wooden balls 3.
- water 5 is preferably fed into the bioreactor 0 via a feed line in the cover 1.3 during the mixing process.
- the dry fractions of the biogenic residues 4 are thus slurried and slurried.
- the biogenic residues 4 enriched with water 5 then successively form biofilms on the surfaces of the wooden balls 3 during the mixing process.
- a suitable magnetic reagent is added, which converts the phosphorus into a magnetic compound.
- an iron salt is added to the water 5 during the mixing process, so that phosphates dissolved therewith are spontaneously precipitated as iron phosphate in the wet biofilms.
- the bioreactor 0 shown in FIG. 2 shows the state after the successful formation of biofilms on the surfaces of the wooden balls 3.
- the fill level in the bioreactor 0 rises to H wet due to the biofilms.
- the wet biofilm is dried.
- the drying takes place by supplying warm air and/or unsaturated, superheated water vapor into the spherical matrix via the surfaces of the biofilms, preferably continuously via all air supply lines and/or steam supply lines 6, 6.1, 6.2 and 6.3.
- the air saturated with water vapor and/or the excess steam is discharged via the exhaust air line and/or the steam discharge line 7 in the cover 1.3.
- the operation of the auger 2 is preferably intermittent.
- the auger 2 is preferably stopped for about 3-60 minutes, particularly preferably 30-60 minutes, and then started to rotate for preferably 10-30 seconds each time.
- the intervals chosen are directly dependent on the heat energy fed into the bioreactor for drying.
- unsaturated, superheated steam is supplied as a drying medium, a quasi-continuous operation of the mixer.
- the biofilms on the surfaces of the wooden balls 3 are homogenized by the mechanical friction process, so that the moisture in the biofilms is distributed largely evenly on all ball surfaces and the effective surface area for evaporation is thus optimized.
- the aim of the drying process is the formation of solid, dry crusts 4.1 of solids on the surfaces of the wooden balls 3.
- the crusts should increase the diameter of the wooden balls 3 preferably in the range from 5% to 10%. This reference value enables the calculation of the mass of solids to be fed preferably and thus also the fresh mass of biogenic residues.
- the biogenic residues are preferably fed in in several partial portions.
- each additional partial portion of biogenic residues 4 is preferably supplied after the biofilms on the wooden balls 3 have partially dried, which have formed as a result of the biogenic residues 4 being supplied.
- the biofilms are dried so that solid, dry crusts form on the surfaces of the wooden balls 3 .
- FIG. 3 shows the bioreactor 0 filled with wooden balls 3 on which solid, dry crusts 4.1 have formed. The filling level has dropped slightly and results in
- the bottom ventilation and/or the steam supply line 6.3 and the lower lateral ventilation and/or steam supply line 6 are now switched off in order to prevent increasingly settled powder 4.2 from being stirred up in the bottom area of the bioreactor 0.
- the aeration and/or supply of steam takes place through the ball matrix, preferably continuously with supplied warm air and/or supplied unsaturated, superheated steam via the air line and/or steam supply line 6.1.
- leakage air and/or leakage steam is preferably fed in via the air inlet line and/or steam inlet line 6.2 and the exhaust air and/or the excess steam is continuously discharged via the outlet air line and/or steam outlet line 7.
- the operation of the auger 2 is also preferably intermittent.
- the screw 2 is preferably stopped for around 3 to 60 minutes, particularly preferably 30 to 60 minutes, and then started to rotate for preferably 10 to 30 seconds.
- the dry crusts 4.1 on the surfaces of the wooden balls 3 are successively removed by friction as a result of the mechanical friction process.
- the coarse and partially fine powder particles 4.2 already in the bioreactor are ground into a fine powder by friction between the surfaces of the wooden balls 3, which has a grain size of less than 100 ⁇ m.
- the process of separating the powder particles is supported by drying the powder in addition to the grinding process. Since the initially dry particles lose their low residual moisture content and thus become powder-dry, a gradual separation of particles that were previously adhesively bonded with water is made possible.
- the powder drying process takes place indirectly via the surfaces of the wooden balls 3 by capillary suction forces, which compensate for small moisture differences between the powder particles and the surfaces of the wooden balls 3 .
- drier and wetter wooden balls 3 are intermittently exchanged between the upper area of the bioreactor 0 and the powder 4.2. This allows the powder 4.2 to be dried with a dry residue content of up to 98% by weight and thus a water content of around 2% by weight.
- FIG. 4 shows the bioreactor 0 filled with wooden balls 3, the surfaces of which have been freed from solids, and powder 4.2 on the bottom 1.1 of the bioreactor.
- the level has dropped slightly to a level Hp UiVer .
- the powder 4.2 can now be drawn off via the discharge device 8.
- the powder 4.2 can be discharged in any desired manner.
- the fine powder with a diameter ⁇ 100 ⁇ m there is often a proportion of up to around 15% of the total weight of larger particles.
- This is dry matter in the form of spherical particles or other forms known as free-flowing substances are also discharged via the discharge unit 8.
- the size of the discharged solid particles depends on the selected discharge device and can range from 1 mm to several centimetres.
- the powder 4.2 of the dry matter 4.1 is often present as a heterogeneous mixture of particles with small diameters and coarser components with a diameter >100 ⁇ m.
- the powdery dry mass 4.2 including the coarser components is therefore advantageously discharged pneumatically by suction air and/or vacuum and the coarser components are then separated from the air flow and/or extracted gas flow (steam flow) with the aid of cyclones.
- an air classifying baffle may be used in the air flow and/or gas flow.
- a perforated plate is preferably provided as a sieve in front of the discharge opening in the peripheral wall 1.2 of the bioreactor 0. In this way, the maximum size of the particles discharged from the container can be determined and the wooden balls 3 can thus be held back.
- the perforated perforated plate is preferably protected from the rotating balls by a cover on the inside of the peripheral wall 1.2 of the bioreactor 0. If the holes are not covered, the holes will be clogged with liquid from the supplied biogenic residues and then harden. An opening is then only possible mechanically with a drill or a chisel. This procedure also applies analogously to other discharge devices, which therefore preferably have to be protected by a cover to the interior of the bioreactor.
- the reactor 0 described above can be part of the plant according to the invention for separating the magnetic, phosphorus-containing compound 4.3 from the dry matter 4.1.
- the dry matter 4.1 thus obtained in the reactor 0 in the form of a powder 4.2 is then fed to a separation device for magnetic separation of the magnetic, phosphorus-containing compound.
- This separation device is described in the following FIGS. 5 and 6 by way of example.
- FIG. 5 shows such a separator for separating magnetic particles, in particular iron phosphate.
- the separator comprises an optional comminution unit 20, a hopper 21, a fall housing (down pipe) 22 with an angled baffle plate 23 and a magnetic device 24 and a storage container 26, which can be arranged in a housing, not shown.
- the dry mass 4.1 obtained from the reactor 0 is fed to the separator in the form of powder 4.2, which also contains the magnetic, phosphorus-containing compound 4.3.
- the powder is 4.2 in the optional crushing unit 20 for homogeneous mechanical grinding to powder 4.2. This makes sense if the coarser dry matter particles with a diameter > 100 ⁇ m have not been separated from the powder 4.2 beforehand or if the dry matter 4.1 is obtained from a process other than bioreactor 0, in which a sufficiently small particle size was not obtained.
- the comminution unit 20 can have a mechanical grinder, for example a cone grinder or a disc grinder or the like.
- the entire mass which is now largely homogeneous as a fine powder 4.2, falls through the funnel 21 below and then in free fall into the downpipe 22 and hits the angled impact plate 23 there the baffle plate 23 swirls the powder 4.2 into a powder cloud and then continues to fall in free fall along the inner drop pipe wall.
- the magnetic device 24 is arranged from the outside, preferably in the form of electromagnets. When energized appropriately, the electromagnets generate a magnetic field 25 which acts in the interior of the downpipe.
- magnetic metal compounds of the phosphorus 4.3 for example iron phosphate, are magnetically attracted to the downpipe wall from the inside and are thus removed from the remaining non-magnetic powder 4.2.
- the powder 4.2 freed from magnetic metal compounds 4.3 continues to fall in free fall into the storage container 26 located below the downpipe 22 and settles there in the floor area.
- An alternative process can be that the substances discharged from the bioreactor 0 are treated separately.
- the coarse dry matter particles with a diameter >100 ⁇ m can be ground up with the crushing unit 20 and then separated magnetically from the iron phosphate in the magnetic separator.
- the fine portion of powder 4.2 with a diameter of ⁇ 100 ⁇ m can be fed directly to the magnetic separator and separated magnetically from the iron phosphate.
- Figure 6 shows the separator as previously described in Figure 5, but the storage container 26 has been set aside and the storage container 27 is now located under the downpipe 22 to accommodate the separated magnetic, phosphorus-containing compound (e.g. iron phosphate particles) 4.3 is the magnetic field 25 generating electromagnet 24 has been turned off, so that the magnetic Metal compounds 4.3 fall in free fall into the storage container 27 and settle there in the bottom area.
- the magnetic, phosphorus-containing compound (for example iron phosphate particles) 4.3 and the remaining dry mass 4.1 are received and collected separately from one another in the storage containers 27 and 26, respectively.
- Storage tank 27 Storage tank 30.1 Housing wall A axis
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Microbiology (AREA)
- Molecular Biology (AREA)
- Health & Medical Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Drying Of Solid Materials (AREA)
- Accessories For Mixers (AREA)
- Mixers Of The Rotary Stirring Type (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2023581041A JP2024525517A (ja) | 2021-07-02 | 2022-07-01 | 生物起源残渣を好適に乾燥させる方法、およびその方法を実行するためのバイオリアクター |
EP22744153.2A EP4363382A1 (de) | 2021-07-02 | 2022-07-01 | Verfahren zum trocknen von vorzugsweise biogenen reststoffen und bioreaktor zur durchführung des verfahrens |
CA3225566A CA3225566A1 (en) | 2021-07-02 | 2022-07-01 | Method for drying preferably biogenic residues, and bioreactor for carrying out the method |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102021116025 | 2021-07-02 | ||
DE102021116025.1 | 2021-07-02 | ||
DE102021122391.1 | 2021-08-30 | ||
DE102021122391.1A DE102021122391A1 (de) | 2021-07-02 | 2021-08-30 | Verfahren zum Trocknen von vorzugsweise biogenen Reststoffen und Bioreaktor zur Durchführung des Verfahrens |
DE102021123157.4A DE102021123157A1 (de) | 2021-09-07 | 2021-09-07 | Verfahren zum Dampftrocknen von vorzugsweise biogenen Reststoffen und Bioreaktor zur Durchführung des Verfahrens |
DE102021123157.4 | 2021-09-07 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2023275377A1 true WO2023275377A1 (de) | 2023-01-05 |
Family
ID=82611098
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2022/068321 WO2023275377A1 (de) | 2021-07-02 | 2022-07-01 | Verfahren zum trocknen von vorzugsweise biogenen reststoffen und bioreaktor zur durchführung des verfahrens |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP4363382A1 (de) |
JP (1) | JP2024525517A (de) |
CA (1) | CA3225566A1 (de) |
WO (1) | WO2023275377A1 (de) |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4999930A (en) * | 1988-05-21 | 1991-03-19 | Kabushiki Kaisha Hikoma Seisakusho | Raw sewage drying apparatus |
JP2001324269A (ja) * | 2000-05-17 | 2001-11-22 | Mitsubishi Kakoki Kaisha Ltd | 伝熱式竪型乾燥装置 |
WO2008095685A2 (de) * | 2007-02-06 | 2008-08-14 | Enthal Haustechnik Gmbh | Vorrichtung und verfahren zum trocknen von gärresten |
-
2022
- 2022-07-01 JP JP2023581041A patent/JP2024525517A/ja active Pending
- 2022-07-01 CA CA3225566A patent/CA3225566A1/en active Pending
- 2022-07-01 EP EP22744153.2A patent/EP4363382A1/de active Pending
- 2022-07-01 WO PCT/EP2022/068321 patent/WO2023275377A1/de active Application Filing
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4999930A (en) * | 1988-05-21 | 1991-03-19 | Kabushiki Kaisha Hikoma Seisakusho | Raw sewage drying apparatus |
JP2001324269A (ja) * | 2000-05-17 | 2001-11-22 | Mitsubishi Kakoki Kaisha Ltd | 伝熱式竪型乾燥装置 |
WO2008095685A2 (de) * | 2007-02-06 | 2008-08-14 | Enthal Haustechnik Gmbh | Vorrichtung und verfahren zum trocknen von gärresten |
Also Published As
Publication number | Publication date |
---|---|
CA3225566A1 (en) | 2023-01-05 |
EP4363382A1 (de) | 2024-05-08 |
JP2024525517A (ja) | 2024-07-12 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DE2908136A1 (de) | Verfahren und vorrichtung zur herstellung von harnstoffkoernchen | |
DE2617811A1 (de) | Verfahren und vorrichtung zum herstellen eines granulats aus einer loesung oder suspension | |
WO2019149405A1 (de) | Pedosphärenverbessernde granulate, herstellungsverfahren und verwendung | |
DE3600400C2 (de) | ||
DE60015398T2 (de) | Verfahren und vorrichtung zur herstellung von teilchen aus einer lösung, einer schmelze, einer emulsion, einem schlamm oder aus feststoffen | |
WO2023275377A1 (de) | Verfahren zum trocknen von vorzugsweise biogenen reststoffen und bioreaktor zur durchführung des verfahrens | |
DE19522164A1 (de) | Verfahren und Vorrichtung zur kontinuierlichen Trocknung von Protein enthaltendem Schlamm | |
WO2023275379A1 (de) | Verfahren und anlage zum abtrennen einer magnetischen, phosphorhaltigen verbindung aus einer trockenmasse durch trockenmagnetscheidung | |
DE102018104877B4 (de) | Vorrichtung und Verfahren zur Trocknung von Feststoff- Flüssigkeits- Gemischen | |
DE102021123157A1 (de) | Verfahren zum Dampftrocknen von vorzugsweise biogenen Reststoffen und Bioreaktor zur Durchführung des Verfahrens | |
DE102021122391A1 (de) | Verfahren zum Trocknen von vorzugsweise biogenen Reststoffen und Bioreaktor zur Durchführung des Verfahrens | |
DE102021122393A1 (de) | Verfahren und Anlage zum Abtrennen einer magnetischen, phosphorhaltigen Verbindung aus einer Trockenmasse durch Trockenmagnetscheidung | |
EP0463546A1 (de) | Verfahren und Vorrichtung zur biologischen Trocknung von Klärschlamm | |
WO2020228905A1 (de) | Ammoniumsulfat enthaltendes düngemittel-granulat sowie vorrichtung, verfahren und stoffgemisch zur dessen herstellung | |
WO2016120317A1 (de) | Verfahren zur konditionierung von düngemittelgranulat | |
WO2020007426A1 (de) | Festes rieselfähiges mehrkomponentengranulat, verfahren zum herstellen eines festen rieselfähigen mehrkomponentengranulates und vollwertiges düngergranulat | |
DE1542425A1 (de) | Verfahren zum Herstellen fester,trockener,koerniger,chemischer Produkte | |
EP3475248A1 (de) | Dipeptidhaltige granulate | |
DE102020130094B3 (de) | Verfahren und Vorrichtung zur Herstellung eines Ammoniumsulfat enthaltenden Düngemittel-Granulats | |
DE2758010A1 (de) | Vollduengemittel zur dauernden biologischen bodenverbesserung und ertragssteigerung sowie verfahren zu deren herstellung | |
DE102013012873A1 (de) | Verfahren zum Aufbereiten von feinkörnigen bis stückigen Ausgangsmaterialien mittels bindemittelfreiem Agglomerieren | |
EP0840714B1 (de) | organisches Düngemittel aus Biomassen-Rückstanden und Verfahren zu seiner Herstellung | |
DE102013112499A1 (de) | Vorrichtung und Verfahren zur Agglomeration der Ablauge eines Cellulosegewinnungsprozesses | |
EP0187118B1 (de) | Verfahren zur Reduzierung des Schadstoffgehaltes im Hausmüll | |
DE102010019100A1 (de) | Verfahren zum Gewinnen von Kalisalz aus einem Zementbypassprodukt in einer Industrieanlage, Verfahren zum Herstellen von Zement, Verfahren zum Gewinnen von Kaliumsulfat sowie Verfahren zum Gewinn von drei unterschiedlichen Salzen |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 22744153 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 3225566 Country of ref document: CA |
|
WWE | Wipo information: entry into national phase |
Ref document number: 18574508 Country of ref document: US |
|
ENP | Entry into the national phase |
Ref document number: 2023581041 Country of ref document: JP Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: 202417003718 Country of ref document: IN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2022744153 Country of ref document: EP |
|
ENP | Entry into the national phase |
Ref document number: 2022744153 Country of ref document: EP Effective date: 20240202 |