Classifications

• • C—CHEMISTRY; METALLURGY
  • C05—FERTILISERS; MANUFACTURE THEREOF
  • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
  • C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
  • C05F17/40—Treatment of liquids or slurries
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E50/00—Technologies for the production of fuel of non-fossil origin
  • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/10—Process efficiency
  • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/141—Feedstock
  • Y02P20/145—Feedstock the feedstock being materials of biological origin
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/50—Improvements relating to the production of bulk chemicals
  • Y02P20/582—Recycling of unreacted starting or intermediate materials
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W30/00—Technologies for solid waste management
  • Y02W30/40—Bio-organic fraction processing; Production of fertilisers from the organic fraction of waste or refuse

Definitions

• the invention relates to a method and a device for the treatment of organic bio-residues, in particular from municipal and / or industrial residues, including raw and / or cooked leftovers, agricultural
• Residues in particular animal excrements and / or plant substances, but also of plant substances specifically grown for the process, in which these substances are at least partially fed to an anaerobic reactor and the biogas resulting from fermentation is thereby withdrawn and the remaining digestate fed to a further use becomes.
• TS dry matter
• the digestate can be continued following a mechanical treatment with a separation for thickening into two partial streams. While the first part stream is subjected to drying for the production of a dry so - called foot fertilizer with a dry matter content of around 85% (TS), the second part stream of the liquid part remaining after pressing undergoes evaporation to produce a so - called head fertilizer with a dry matter content of approx 15%.
• the wet head fertilizer originating from the evaporation of the digestate usually has a nitrogen content of about 6 percent, there is a lack of dry foot fertilizer i.d.R., originating from the drying of the digestate. at a 3% minimum salary.
• this digestate is able to bind, for example, ammonia with the nitrogen contained therein.
• the object of the present invention is now to provide a method and a device of the type mentioned, the / an improved treatment organic residues for the production of a usable substance, eg. As an energy source, but also a recyclable substance in the form of fertilizer as an energy source allows.
• a usable substance eg. As an energy source
• a recyclable substance in the form of fertilizer as an energy source allows.
• the process is also geared to optimizing the energy cycle concerning the processing of renewable raw materials (NaWaRo). Specifically, this is done by a multi-stage vacuum evaporation, which can be assigned a conditioning that works without external energy.
• the core idea of the invention is thus to use the fermentation residue obtained, for example, in the generation of biogas from organic residues in an improved manner by at least partially recombining the fermentation residue cake resulting from the thickening and the liquid stream originating from the thickening, after the fermentation Liquid stream was subjected to a treatment that can be separated from the liquid stream, a concentrate and a condensate. While the condensate consists almost entirely of water, the other ingredients present in the liquid stream are concentrated in the concentrate. With this concentrate thus obtained, the fermentation residue cake can then be enriched again and subjected to further conditioning, for example in the form of drying or pelleting.
• the invention creates an optimal utilization of the digestate, for example, in the generation of biogas by this - where necessary - by the upgraded energy from biogas generation and its power generation.
• the term "revaluation” is understood to mean both better handling by thickening - factor eg 1:10 -, shelf life, usability for heat generation or enrichment with additives, as well as any other processing, eg drying.
• the waste heat arising from the utilization of the biogas is used for drying. If the system is to be operated absolutely autonomously, the available waste heat determines the
• all of the concentrate obtained may be added to the thickened cake and the mixture subsequently dried. It has proven advantageous to supply the concentrate to the foot fertilizer during its drying (which will be explained later in connection with a belt dryer).
• the recovered retentate corresponds to the enriched with the components of the digestate concentrate.
• the mass flow of the fertilizer transferred to the concentrate is at least chosen so that the enriched dry product, ie the foot fertilizer after drying has a minimum content of 3% of nitrogen and / or potassium and / or phosphorus or compounds thereof.
• the product obtained is considered organic fertilizer.
• the conversion of low quality biomass into organic fertilizer for agriculture occurs by accumulating any excess nitrogen, potassium, or phosphate fractions from the digestate processing to the inferior fertilizer stream, i.
• the energy transfer of CHP waste heat to the drying or evaporation is usually done via heat exchangers, by means of which the waste heat is discharged to the evaporator or dryer / conditioner.
• the mass fraction of the wet fertilizer to be supplied during its drying wet head fertilizer is co-determined by the available from the waste heat of the CHP energy amount again.
• Foot fertilizer has at least a minimum content of 3% nitrogen or potassium or phosphate.
• Wet fermenter for biogas generation is possible in which an excess amount of energy in the waste heat of biogas operated Bioflowerkraftwerks is given to operate the drying and evaporation, such that from this excess energy, a mass transfer of head fertilizer to the foot fertilizer in the size range of 20% of the total produced head fertilizer is feasible.
• the constituents of the fermentation residue raw material are subject to a quantity fluctuation, with which also the procedural properties of the digestate raw material can vary. This affects the separability of the solids, which in turn affects the performance of the drying and evaporation and, ultimately, the amount of concentrate produced therefrom. While at a maximum
• the concentrate amount of produced fertilizer is the lowest, increases the amount of concentrate to be removed by increasing the dry matter content after thickening.
• an acid for example, H 2 SO 4 is supplied to bind the per se volatile fraction of nitrogen compounds, such as ammonia in the digestate to be able to. Because of this binding, the proportion of nitrogen in the treated partial streams usually increases in both partial streams, ie in the production of the dry foot fertilizer and in the production of the wet topical fertilizer.
• the binding of these nitrogen compounds in the digestate has the advantage that no odors escape from the digestate, as would be the case, for example, in the outgassing of ammonia from the digestate.
• this addition of sulfuric acid is carried out according to the invention, the thickening of the digestate raw material in the resulting fermentation residue cake inside, as this foaming is prevented. Also, a flotation, ie flooding avoided because the solids are present in the press cake. Should the addition of the acid in the liquid portion of the digestate lead to foaming, foam inhibitors may be used or provided mechanical means for foam inhibition. Intensive experiments have also shown that the residence time and the temperature of the digestate play an important role in foam inhibition. For this reason, dwell containers are interposed and / or a preheat of the
• a screening / fine screening means for example, a vibrating screen of the thickening coming from liquid fraction to
• the final product to be taken from the drying plant has a minimum content of 3% of at least one of these substances, ie it is a fertilizer which is also purely organic on top of that.
• the enrichment of the dry foot fertilizer to a full organic fertilizer has the advantage of a significantly lower odor nuisance compared to a direct discharge of liquid manure on the field. Furthermore, any transport costs are reduced due to the lower weight of a dry fertilizer compared to the digestate substrate as fertilizer.
• a wet fermenter As a fermenter for biogas generation, a wet fermenter can be used, which requires a minimum content of water to ensure a functioning operation, or in other words, a maximum value of dry matter must not be exceeded, depending on the raw material about 10 - 13% dry matter are common.
• the condensate obtained from the evaporation of the top fertilizer or from the drying of the foot fertilizer can be recycled. This recirculation can be metered directly into the mashing or alternatively added to the feed line of the fermenter. If it is condensates containing foam or very volatile substances, a reverse osmosis can be used, in order not to burden the mashing but especially the acidification and fermentation unnecessarily with eg solids and / or salts.
• a dry fermenter can also be used.
• a methanation and biogas production with an increased proportion of supplied dry matter is possible because of the supply of water from, for example, the condensate, which is obtained in the evaporation or drying, can be largely dispensed with. Due to the lower energy required when using a dry fermenter for the evaporation and drying of the digestate, the proportion of transferred increases
• the branch streams of foot fertilizer on the one hand and head fertilizer resulting after the mechanical treatment can, on the other hand, largely be brought together again.
• the originating from the drying fertilizer as a high-quality fertilizer and a utilization of the foot fertilizer can be provided in the form of a gasification for the production of an energetically valuable gas.
• the gasification is explained below in the context of the description of a "secondary cycle" of the invention.
• the above basic cycle for upgrading inferior biomass to organic fertilizer is followed by an additional secondary circuit, which is described below - the statements made above with regard to the basic cycle, however, apply analogously to the secondary cycle.
• the dry fraction of manure is pressed into pellets in a downstream pelletizing system by means of a pelleting press.
• a pelleting press Alternatively, an extruder may be used.
• This secondary cycle is particularly advantageous if the organic fertilizer produced has a non-usable as fertilizer excess.
• the recovered organic fertilizer is revalued again as a usable raw material by instead of the original energy carrier fertilizer, a new energy source in the form of further processable pellets is obtained.
• the energy required for pelleting can be taken from the energy obtained from the bio-cogeneration plant. In order to take the energy requirement into account again, that the upgrading of the original digestate must be carried out with energy generated from the utilization of the biogas, it is expedient to provide a dry fermenter for the generation of biogas in the downstream pelletizing:
• the pellet combustion can be interposed a steam turbine, which in turn operates a generator, which then emits the electrical energy obtained in the power grid of the CHP.
• a gas turbine or a piston engine interposed, which likewise emits electrical energy via a generator operation in the power grid of the base CHP's.
• ash (combustion) and coal (gasification) can be used as fertilizer.
• a multivergaser is provided for the gasification, which can be fed with different materials for gasification.
• the plant can also be adapted to fluctuating raw material crops, for example by a low-yielding maize crop is at least partially compensated by the addition of wood and thus an energy supply is ensured due to drought.
• total cycle - the statements made above in relation to the basic circuit, however, apply analogously to the total cycle:
• the focus in the utilization of the dry matter obtained from the organic fertilizer is in a gasification.
• the result recovered gas is now mixed according to the invention the biogas, so that electric energy is obtained from this mixture in Bioflowerkraftwerk. Due to this measure, the energy balance in the direction of a higher energy yield can be postponed, among other things, since the efficiency " ⁇ " is higher in energy production from the biogas / gas mixture in the CHP, as each of the efficiency at
• total cycle is equivalent to the "second circuit 1
• mass flow of transferred topical fertilizer into the topical fertilizer can be increased equally - as described above for the exemplary embodiment of the "secondary cycle” - up to 100%.
• additional electrical energy is generated, so that about 35% more electrical energy can be obtained from the same country or its Nawarro values, which is crucial in view of the expected scarcity of raw materials.
• the gas produced in the gasification still has components that are detrimental to further utilization of the gas, such as mainly nitrogen compounds, which in the process of utilization of the gas to NO x and
• the gas is purified, namely by being advantageously at least partially passed through the accumulating during the thickening liquid portion of the digestate. Another partial flow of the gas can also be passed through the concentrate or condensate for its purification. Experiments have shown that the harmful for the utilization of the gas components are deposited.
• the purified gas can then be supplied either by means of a gas turbine or piston engine power generation or it is advantageously added to the gas obtained during the fermentation.
• the nitrogen content of the gas obtained in the gasification of the foot fertilizer or pellets are returned by the deposition process in the liquid content of the digestate or in the concentrate from the evaporation, the latter is enriched with precisely these deposited components again, bringing it to the revaluation of low-grade fertilizer useful for organic fertilizer. If the gas is passed through the condensate, this can also be added directly to the fertilizer stream
• the gas formed during the gasification can also be purified, at least temporarily, by passing it through the condensate formed during the evaporation.
• This measure is useful if the mass flow of top dressing to foot fertilizer is approximately 100% and at the same time the obtained fertilizer is to supply at least for a certain period of time exclusively to a gasification.
• the invention in the context of the utilization of the foot fertilizer by gasification, a two-stage gas generation from biogas fermentation and optimized gasification of the digestate created, which gas generation consists of two independent gas flows.
• the invention provides a maximization of energy yield while concentrating recyclable recyclable recyclables from the original starting substrate.
• This combination increases the flexibility of the process as needed for more energy or more fertilizer.
• the residue coming from the gasification also with top dressing or the partial flow of condensate used for cleaning can be enriched, so that the resulting product again meets the requirements of an organic fertilizer, so that the residue from the gasification can be discharged as it were agricultural.
• FIG. 2 shows the method according to the invention in accordance with the so-called second circuit
• FIG. 3 shows the method according to the invention according to the so-called total cycle
• FIG. - Fig. 4 shows an advantageous belt drying system according to the invention.
• the pre-acidification serves to dissolve complex carbon compounds, since the fermentation bacteria of the subsequent fermentation (III) only Preferably degrade simple carbon compounds. Typically, the pre-acidification must reach a pH of 6.0 or below.
• the residence time of the loaded input substrate in the pre-acidification depends on the digestion time of the individual constituents. For example, press residues such as solid peel pieces require a longer residence time compared to organically loaded fluid.
• the starting substrate in particular maize or other silages, it is advantageous to allow the starting substrate, in particular maize or other silages, to rest slightly stirred in the mashing, so that air can escape.
• This has the advantage that the formation of floating layers in the subsequent fermentation (III) is prevented and an occurring in the processing of the digestate NH 4 formation can run optimized (was explained above).
• the assumption (I) and / or the treatment (II) may also include a grit trap.
• the resulting crude mixture or raw substrate is transferred to the fermentation (III) without any risk of further acidification in the anaerobic fermenter. This would be detrimental to the fermentation process due to damage to the methane bacteria due to the too low pH.
• the process step of fermentation in the anaerobic reactor using acetogenic bacteria and Methanbakterien the
• the dry matter content (TS) of the digestate in the digestate storage is about 5 to 7%.
• the temperature in the fermentation residue storage is about 34 ° C.
• the digestate is fed from the store mechanical pressing for thickening of the same.
• the thickened cake with an increased dry matter content of about 25% which partial flow is referred to as a base fertilizer
• topical fertilizer the obtained from the compression liquid content with a lower dry matter content of approx. 3%, hereinafter referred to as topical fertilizer.
• a foam inhibition in these streams can be done as previously described.
• the head fertilizer is subsequently filtered in vibrating screens to filter ultra-fine fibers that could accumulate during the subsequent evaporation or reverse osmosis with ultrafiltration.
• a solids content falls as a concentrate with a dry matter content of about 10%, which after thickening e.g. by means of a decanter also the dryer VII can be supplied.
• the head fertilizer stream is first preheated from an initial temperature of 29 0 C to about 63 ° C.
• the subsequent evaporation takes place in several vacuum stages advantageously using the waste heat of the CHP.
• drying With regard to the partial flow of the thickened cake this is subjected to drying (VII).
• the conditioning is carried out, for example, in a belt dryer in which the thickened press cake is conveyed on horizontally superimposed belts, so that the cake from the top belt after passing it falls on the underlying belt and in this "zig-zag process" down is promoted to the last volume. Details of the drying process are mentioned in connection with FIG. 4.
• a heat exchanger is provided, with which the waste heat resulting from the Bioflowerkraftwerk is transmitted for this purpose.
• the waste heat temperature of the energy source of the CHP is approximately 145 0 C when entering the
• Dried dried cakes regardless of their constituents and composition as well as their intended purpose, are referred to as foot-dried fertilizers.
• the last condensation stage of the evaporation can deliver the energy. This is particularly advantageous if the fermentation plant only generates feed gas and thus "Energy shortage" prevails. Then, as in any case, the energy shortage can make sense to burn the organic fertilizer for energy production in whole or in part.
• Nitrogen content of about 6% is the
• Nitrogen content of dry foot fertilizer i.d.R. below 3%.
• a part of the head fertilizer concentrate is fed in a controlled mass flow of the foot fertilizer in the belt drying plant.
• This regulated mass flow is u. a. depends on the energy available from the CHP if the process is to be energy-autonomous. Because the available waste heat is used for drying, which therefore the amount of waste heat determines the dry mass and therefore also the wet content, which can be added to the foot fertilizer. In this case, in this case, the mass flow may amount to approximately 20% of the total produced head fertilizer, so that as a result by combining the two partial streams, i.
• Crop fertilizer on the one hand and foot fertilizer on the other hand a high-quality organic fertilizer is produced in solid form, the proportion of nitrogen is above a 3% limit.
• the transfer of topical fertilizer in the topical fertilizer can also affect the potassium or phosphate content in addition to the example shown for nitrogen enrichment of the foot fertilizer.
• Fig. 2 shows schematically the so-called. Secondary circuit in construction to the basic circuit explained above. According to the secondary cycle, the substrate resulting from drying (VII) is further processed, i. subjected to pelleting (K) and / or fed to a subsequent gasification (XI) or combustion (X).
• VI the substrate resulting from drying
• K pelleting
• XI gasification
• X combustion
• Apparatus for compacting the dry material can be used a pelletizer or an extruder.
• This drying substrate has a dry substance content of about 80% on average.
• Those obtained from pelleting (IX) compressed Pellets with about 85% dry matter are fed to a combustion and / or gasification in order to gain electrical energy by means of a fuel cell, a combustion boiler, a reciprocating engine or a gas turbine, which is fed, for example, into the power generation (IV) of the CHP.
• Partly derived from evaporation head fertilizer or condensate partial flow thus leads to a further energetically optimized process management in the recovery of originating from the fermentation residues.
• Fig. 3 schematically illustrates the principle of the so-called. "Total réellelaufs", a
• Continuation of the secondary circuit according to FIG. 2 or a continuation of the basic circuit according to FIG. 1 means.
• the gas originating from the gasification (XI) of the dry substance is mixed with the gas resulting from the fermentation and together fed to the power generation (FV) of the bio-cogeneration plant.
• the gas originating from the gasification of the dry substance is passed through the digestate in the digestate store (V) for cleaning.
• the gas for its purification by the concentrate of the top fertilizer from the evaporation or by the condensate or a partial flow thereof can be performed.
• the gas obtained from the gasification is energetically and ecologically refined if it is guided by, for example, the liquid content of the wet stream produced during the thickening of the digestate.
• this liquid fraction is enriched with nutrients that are unfavorable for the utilization of the gas, but the purification of the gas represents a real qualitative improvement also for the liquid content, since it is enriched with substances, so that it can be used as an organic fertilizer agricultural .
• a passage of the gas through the condensate should, however, only be targeted if the condensate is no longer needed, for example, as water for mashing the silage when entering the fermenter.
• the positively charged currents can also the organic residual fertilizer (not shown) are added. If the condensate still contains nutrients or other substances (eg salts), a reverse osmosis can be used, so as not to pollute the mashing and the subsequent stages.
• the "production costs" of the plant (IV) are optimized, and the energy yield is increased due to the higher efficiency in the mixed gas utilization. While the efficiency of a gas turbine in the gasification of the originating from the drying (VII) dry matter is about 25%, the efficiency of a gas turbine in the gasification of the originating from the drying (VII) dry matter is about 25%, the efficiency of a gas turbine in the gasification of the originating from the drying (VII) dry matter is about 25%, the efficiency of a gas turbine in the gasification of the originating from the drying (VII) dry matter
• Final energy ie purely organic fertilizer, energy in the form of digestate or pellets or electrical energy allows.
• This flexibility also allows optimal adaptation of the entire process engineering plant to the available starting materials. If, if appropriate, a maize harvest intended for feeding the plant fails to be sufficient, the plant can be operated in the multivergator due to the multitrack process options with other substances, eg with green waste or wood for gasification. By adapting to fluctuations in the raw material and the energy demand, there is also an adaptation of the plant to different location needs. With others Words is created by the flexibility created by the method, a plant described above at any geographical location useful.
• the dryer (VII) and evaporator (VIII) systems are associated with a refrigeration unit and a heating unit - not shown - to be used purely for e.g. as a control unit to compensate for the fluctuating energy requirements at startup, as well as performance changes u.a. to reconcile with the current supply of electricity from the CHP.
• FIG. 4 schematically shows a belt drying plant, as used for the
• Drying of the fertilizer coming from the thickening of a fermentation residue and a head fertilizer resulting from the evaporation can be used in an advantageous manner. It is important that the dryer not only as usual "to the shelf life" should lead, but promotes for all subsequent steps, such as pelletizing or gasification produces the optimally required residual moisture.
• the conditioner 10 has a drying space 12 through which material is transported from a starting point 20 of the drying space to an end point 22 thereof.
• the conditioning itself is effected by means of exhaust air, wherein the sucked through the drying chamber 12 air absorbs the moisture of the wet mixture and dissipates it.
• the exhaust air outlets 14 shown in FIG. 4 are followed by exhaust air pumps (not shown).
• the heat energy required for drying is usually taken from the waste heat of Bioschreibkraftmaschinees, but can also in addition by heating means (not shown) of the conditioner or e.g. also be made available from the final stage of the evaporator. Also, the
• the material to be dried itself consists of a first wet mixture, namely the fertilizer coming from the mechanical thickening, which substance content of about 75%, and a second wet mixture, the so-called head fertilizer from the evaporation with a dry matter content of about 15% DM.
• the first wet mixture i. the foot fertilizer is supplied to a first wet goods inlet 24 of the belt drying plant.
• a distribution rake (not shown) may be provided.
• the first wet batch is transported on a top conveyor belt 16 in the longitudinal direction of the drying space 12 horizontally therethrough until the wet mass at the end of the conveyor belt via a chute (not shown in detail) falls on the underlying follower belt.
• the first wet batch thus takes a conveying path 18 from the starting point 20 to the end point 22 of the drying chamber 12, which conveying path 18 is shown in FIG. 4 with a thick solid line.
• the product is discharged 30 of the dry material.
• the belt drying plant shown has five vertically superimposed conveyor belts.
• the speed of each band can be controlled separately with, for example, a frequency converter continuously.
• the conditioner can be optimally adapted to the product to be dried.
• conveyor belts 16 and filter belts with different mesh size can be provided.
• the head fertilizer On the first wet batch, ie the foot fertilizer, is now after half a run of the same through the drying room 12 a second wet mass, ie the head fertilizer "excited".
• the second wet batch is brought into the drying chamber 12 via a second feed 32 for the second wet batch. Since the dry matter content of the head fertilizer is so low that this as a fluid through Tubes is conveyed, the head fertilizer is transported by means of pipes 28 in the drying room 12.
• Openings of the head fertilizer is applied to the first carried on the respective conveyor belt wet mass.
• the exit amount of the head fertilizer at the respective second wet product inlet 26, i. the respective outlet nozzle is controlled in an advantageous manner by means of valves.
• the product delivery 30 then takes place from dry material, consisting of dried foot-applied fertilizer and dried topical fertilizer, which dried mixture has a dry matter content of about 80%.
• This dried material can be applied both as a fertilizer agricultural, or it can be subjected to further processing, for example, a gasification in an advantageous manner to energetically recoverable from the material to be dried
• This gas can be added to the fermentation originating biogas.
• drying of foot fertilizer in the conditioner according to the invention can also take place without the addition of the head fertilizer.

Landscapes

• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Life Sciences & Earth Sciences (AREA)
• Engineering & Computer Science (AREA)
• Biochemistry (AREA)
• Biotechnology (AREA)
• Health & Medical Sciences (AREA)
• General Chemical & Material Sciences (AREA)
• Microbiology (AREA)
• Molecular Biology (AREA)
• Organic Chemistry (AREA)
• Processing Of Solid Wastes (AREA)
• Fertilizers (AREA)

Applications Claiming Priority (3)

Publications (1)

Family

ID=39477794

Family Applications (1)

Country Status (5)

Families Citing this family (27)

Family Cites Families (17)

• 2007
  • 2007-01-31 DE DE200710004892 patent/DE102007004892A1/de not_active Withdrawn
• 2008
  • 2008-01-04 US US12/522,144 patent/US20100071429A1/en not_active Abandoned
  • 2008-01-04 DE DE200811000570 patent/DE112008000570A5/de not_active Withdrawn
  • 2008-01-04 WO PCT/DE2008/000007 patent/WO2008080394A2/de not_active Ceased
  • 2008-01-04 BR BRPI0806494 patent/BRPI0806494A2/pt not_active IP Right Cessation
  • 2008-01-04 EP EP08706725A patent/EP2099726A2/de not_active Withdrawn

Non-Patent Citations (1)

Also Published As

Similar Documents

Legal Events