WO2008128776A2 - Procédé de purification de biogaz et biogaz pouvant être ainsi préparé - Google Patents

Procédé de purification de biogaz et biogaz pouvant être ainsi préparé Download PDF

Info

Publication number
WO2008128776A2
WO2008128776A2 PCT/EP2008/003286 EP2008003286W WO2008128776A2 WO 2008128776 A2 WO2008128776 A2 WO 2008128776A2 EP 2008003286 W EP2008003286 W EP 2008003286W WO 2008128776 A2 WO2008128776 A2 WO 2008128776A2
Authority
WO
WIPO (PCT)
Prior art keywords
biogas
caco
depletion
dehydrated
cao
Prior art date
Application number
PCT/EP2008/003286
Other languages
German (de)
English (en)
Other versions
WO2008128776A3 (fr
Inventor
Heinrich Follmann
Original Assignee
Heinrich Follmann
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Heinrich Follmann filed Critical Heinrich Follmann
Priority to EP08749085A priority Critical patent/EP2139831A2/fr
Publication of WO2008128776A2 publication Critical patent/WO2008128776A2/fr
Publication of WO2008128776A3 publication Critical patent/WO2008128776A3/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
    • C12P5/023—Methane
    • 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
    • Y02P20/141—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
    • 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 present invention relates to a process for the purification of biogas, biogas producible thereby, as well as to processes for the production of a fertilizer and / or soil improver and to a fertilizer or soil improver which can be produced therewith.
  • biogas which typically contains about 58 to 62% methane, about 38 to 40% CO 2 , 0.1% to 0.5% H 2 S and traces of O 2 , N 2 and siloxanes and beyond a has a certain water content of about 2.7 to 3.1% water content, the comparatively high CO 2 content and the water content preclude.
  • the present invention is therefore based on the object to provide a method for the purification of biogas, which is associated with a low expenditure on equipment.
  • Another object of the present invention is to provide a method for purifying biogas, which can be operated with a low energy cost.
  • the depletion liquid depletes CO 2 and / or H 2 S from the biogas and the depletion liquid comprises Ca (OH) 2 .
  • the object is more precisely achieved in a first aspect by a method for purifying biogas comprising the steps:
  • the depletion liquid depletes CO 2 and / or H 2 S from the biogas
  • the depletion fluid comprises Ca (OH) 2 .
  • reaction conditions in conjunction with the design details of the gassing system, are selected and adjusted to produce crystalline CaCO 3 as the reaction end product.
  • the H 2 S is converted to CaS and / or CaSO 4 .
  • the depletion liquid is contained in a carboxylation reactor and / or the reaction of CO 2 and / or H 2 S takes place in the carboxylation reactor.
  • the biogas originates from a fermentation process, preferably an anaerobic fermentation process.
  • the biogas prior to purification has a composition as follows:
  • biogas before being passed through the biogas by the depletion liquid is optionally subjected to a pre-acidification with separation of the H 2 and CO 2 formed thereby.
  • the biogas after depletion, has a methane content of 85 or more vol%, preferably 90 or more vol%.
  • the biogas after depletion, has an H 2 S content of less than 50 to 20 mg per m 3 .
  • the Ca (OH) 2 is an aqueous solution of CaO, preferably slaked lime.
  • the slaked lime is made from CaO, in particular technical quicklime.
  • the technical quicklime as used herein, is a quicklime that still contains about 5-10% impurities.
  • the impurities are of a chemical nature and consist essentially of magnesium, iron and manganese compounds.
  • at least part of the removal liquid is produced by reacting the biogas containing depleted water, after step b), with CaO or hydrated lime, in particular technical slaked lime, as described herein, or Ca (OH) 2 .
  • the depleted after step b) biogas preferably still contains about 5-7% CO 2 .
  • the biogas is controlled and / or homogeneously added to the depletion liquid.
  • the entry of the biogas by means of a Gaseintragungsstoff wherein the Gaseintragungsstoff is preferably selected from the group comprising a fast-rotating high-speed self-priming gas turbine or a slowly rotating pre-pressure working gas turbine.
  • the gas introduction means is a radiant tube ventilation system with distribution stirrer or circulation pump, or a jet tube ventilation system without distribution stirrer and without circulation pump.
  • the crystalline CaCO 3 is decanted.
  • the depletion of CO 2 and / or H 2 S is continuous.
  • the depletion of CO 2 and / or H 2 S is discontinuous.
  • the biogas after depletion, is passed through a humidification reactor filled with CaO, preferably technical CaO or Ca (OH) 2 , substantially all of the water present in the biogas through the CaO or Ca (OH) 2 to form Ca. (OH) 2 or CaCO 3 is absorbed, so that in the end a complete drying of the biogas takes place. Furthermore, in the same step, residues of CO 2 still present in the biogas are simultaneously absorbed in the range between 80-95% of the residues present. In one embodiment, the CaCO 3 is regenerated, preferably to CaO.
  • the object is achieved in a second aspect by a biogas produced by a method of the first aspect, preferably characterized in that any substances present from the group of siloxanes are also quasi quantitatively removed.
  • the object is achieved in a third aspect by a method for producing a fertilizer and / or soil conditioner comprising the following steps:
  • the depletion liquid comprises Ca (OH) 2 and the depletion liquid depletes CO 2 and / or H 2 S from the biogas,
  • the CaCO 3 thus obtained is mixed with fermentation residues, preferably aerated fermentation residues from a fermentation process.
  • the fermentation process generates the biogas.
  • the fermentation residues originate from an anaerobic fermentation process and are preferably concentrated fermentation residues.
  • the fermentation residues contain 5 to 20 kg nitrogen / m 3 digestate concentrate and / or 1 to 4 kg phosphorus per m 3 digestate concentrate.
  • the mixture of CaCO 3 and digestate is dewatered, preferably using a device selected from the group comprising belt filters, vacuum filters, drum filters, vacuum drum filters, filter presses, vacuum filter presses, centrifuges, and decanters for dewatering.
  • the object is achieved in a fourth aspect by a soil conditioner or fertilizer, preparable according to a method of the third aspect.
  • the soil conditioner has the following composition:
  • the soil conditioner preferably
  • (a) contains a weight fraction of dehydrated digestate and one-half weight fraction of dehydrated CaCO 3 , or
  • (b) contains a weight fraction of dehydrated digestate and one to four parts of dehydrated CaCO 3 ;
  • the proportion of CaCO 3 on the mixture of dehydrated CaCO 3 and dehydrated digestate as contained in or forming the soil improver is 10% by weight or less.
  • the comparatively small proportion of CaCO 3 serves as a substitute for the addition of otherwise required flocculation aids.
  • the inventive method allows effective removal of CO 2 - contained in biogas and F ⁇ S amounts and optionally also contained siloxanes. It is particularly noteworthy that the removal of the essential components of the CO 2 and H 2 S takes place substantially simultaneously, ie with the introduction or passage of the biogas through the depletion liquid.
  • the process control and in particular the passing of the biogas through the depletion liquid is carried out so that homogeneous crystals of defined size, preferably in the range between 10 microns and 50 microns form.
  • homogeneous crystals of defined size preferably in the range between 10 microns and 50 microns form.
  • process parameters which lead to the formation of such CaC0 3 crystals are known to those skilled in the art and vary depending on the actual reaction vessels used and the dynamic parameters of the ventilation system used, in conjunction with the liquid circulation characteristics.
  • biogas as used herein preferably refers to a methane-containing gas produced from native and / or municipal wastes by fermentation or fermentation Biogas is preferably particularly different from natural gas obtained from fossil deposits.
  • biogas qualities with a methane content of 90 to 98% are achieved.
  • the hydrogen sulfide contained in biogas is quasi completely absorbed according to the method according to the invention and for the most part converted into CaS and to a lesser extent to CaSO 4 .
  • the reaction of the biogas with depletion fluid is typically carried out in a reaction vessel containing the depletion fluid.
  • the present inventor assumes that part of the Ca (OH) 2 is dissolved in accordance with its pH and temperature-dependent solubility and reacts with the CO 2 contained in the biogas to form CaCO 3 with evolution of heat ,
  • the amount and concentration of Ca (OH) 2 in the reactor, the biogas flow rate, the speed and design parameters, as well as the fluid circulation of the turbine typically used for biogas input can be adjusted within the knowledge of those skilled in the art.
  • the conversion of CO 2 contained in the biogas is controlled with the depletion liquid so that the CaCO 3 is obtained in a particularly advantageous for later processing microcrystalline crystal structure.
  • the process according to the invention can either be carried out batchwise until complete reaction of the Ca (OH) 2 present in the reactor to CaCO 3 or continuously.
  • continuous operation a certain amount of unconsumed Ca (OH) 2 solution is added to the reaction vessel and simultaneously withdrawn a certain amount of the reaction product CaCO 3 .
  • the removal of H 2 S due to its significantly lower concentration in the biogas is typically not the inventive method or the mode of operation limiting factor.
  • due to the solubility of G 2 H practically guaranteed a quantitative distance from the biogas. This also applies to the existing in certain biogas qualities siloxanes.
  • Siloxane-containing biogas types are in particular landfill gases, which in a preferred embodiment also fall within the term biogas, and biogas from plants based on cereals, wherein the siloxanes are typically formed from the silicon contained in the husks of the cereal.
  • siloxanes which are added as hydrophobing agents to inorganic building blocks such as CaCO 3 with their hydrophilic chains to the outer Structure of the crystalline precipitated calcium carbonate attach, whereas the hydrophobic chain ends point to the outside. If, therefore, siloxanes are present in the biogas, they are bound to the surface by the precipitated calcium carbonate or the special crystals obtained by the process according to the invention.
  • the term "quasi-quantitatively removed” means that about 95% or more of the input and concentration of the particular substance or compound (s) are removed.
  • the solution of Ca (OH) 2 used as a depletion liquid is preferably produced by controlled "quenching" of crystalline CaO or by addition of water to Ca (OH) 2 in an extinguishing reactor
  • the heat of reaction of this strongly exothermic reaction is used for heating domestic water or For producing steam, which can be used for the operation of the plant on which the process according to the invention runs, in the context of the present invention it is preferred to use crystalline CaO, also called burnt lime, for the production of the depletion liquid.
  • a batch is typically completed, as can be determined by the temperature increase of this exothermic reaction, the increase of the pH or the change of the conductivity. Thereafter, the reactor is completely emptied, new with about 20 wt .-% dilute Ca (OH) 2 - solution loaded, and the reaction started again. In the Ausletationsgszeit is typically switched to a parallel reactor. Preferably, a batch is designed to last about 60 to 90 minutes.
  • the biogas thus obtained can be fed into existing natural gas networks in the virtually absence of H 2 S and / or siloxanes after conditioning and used by conventional gas engines, gas turbines and / or gas burners, which generally with a lower design cost and a higher efficiency are connected as special for biogas modified gas engines, gas turbines and / or gas burners.
  • Conditioning is preferably understood to mean the process in which biogas is admixed with a propane fraction which is customary for natural gas and with odorizing agents.
  • CaCO 3 can be recycled back into the reaction cycle itself. For example, by using a kiln from the obtained CaCO 3 again CaO can be formed to release CO 2 .
  • the CaCO 3 can be used as fertilizer or soil conditioner, in particular after addition of appropriate additives.
  • Particularly suitable additives in this respect are fermentation residues, in particular fermentation residues from an anaerobic process, wherein preferably the biogas to be purified according to the invention originates from such an anaerobic process.
  • the fermentation residues obtained in the anaerobic process are preferably aerated and more preferably concentrated.
  • Typical concentrated fermentation residues contain 5 to 20 kg N, 1 to 4 kg P per m 3 and other valuable substances such as all trace elements in biologically well-usable form, S compounds, all macroelements such as Mg, K, B, humic acids and vitamins.
  • the CaCO 3 formed in the context of the method according to the invention is also advantageous because it is the process control of the subsequent process steps for the preparation of soil conditioners or fertilizers significantly influenced.
  • the processes for the preparation of soil conditioners or fertilizers can be simplified insofar as the CaCO 3 obtained according to the invention is subjected to the centrifuging operations to which the fermentation residues or fermentation residues to be concentrated or dehydrated as CaCO 3 are to be dehydrated , which can practically replace the polyelectrolytes otherwise required for the sedimentation process, whereby on the one hand the use of the same and on the other hand also corresponding process steps are dispensed with.
  • the fermentation residues before mixing with the CaCO 3 contained in the process according to the invention preferably contain 10% or more dry matter. After mixing with the CaCO 3 , the mixture is concentrated to a dry matter content of about 25 to 50%.
  • the end product thus contained thus represents a thickened, high-quality lime fertilizer, which is enriched with N, P, K and S, organic material and other trace elements.
  • the final product is already storable and transportable and can, inter alia, in the field of agriculture, but also used for other purposes, such as for the backfilling of mine tunnels or landfills.
  • a particularly preferred mixture of CaCO 3 and concentrated digestate results from the typical mass balance of a biogas plant starting from, for example, vinasse from biotethanol production, wherein grain is used as raw or starting material.
  • a mixture comprises: a weight portion concentrated largely dehydrated fermentation residues, preferably with about 25 to 30% dry matter; half a part by weight of dehydrated CaCO 3 , preferably about 40 to 50% dry matter
  • the mixture then has the following composition with regard to its most important elements:
  • FIG 3 shows an exemplary system for operating the reaction vessel required for carrying out the method according to the invention.
  • Fig. 1 shows a reaction vessel 1 containing the depletion liquid 2 comprising Ca (OH) 2 .
  • the biogas originating from an anaerobic fermentation process is conducted via line 3 to the bottom of the reaction vessel 1 and there to a turbine 4, which operates in the illustrated embodiment preferably according to the principle rotor stator and controls the biogas and homogeneously distributed in the liquid phase of the depletion liquid 2 .
  • a turbine 4 which operates in the illustrated embodiment preferably according to the principle rotor stator and controls the biogas and homogeneously distributed in the liquid phase of the depletion liquid 2 .
  • Such devices for the introduction of gas are known in the art and may for example be Frings turbines or other systems, such as a ring ventilation in combination with a high-performance stirrer, or even simple Strahlrohrbel legislative hinssysteme without further additional rheological distribution systems.
  • the reaction vessel 1 further comprises an outlet conduit 6 which is connected to pump 7 which transports the CaCO 3 , more precisely the sludge settling at the bottom of the reaction vessel, to a filter or separation device 8 in which the CaCO 3 is separated from the depletion liquid contained in the sludge.
  • the separated depletion liquid is then passed via a further line 9 into an extinguishing reactor 17 (not shown in FIG. 1).
  • the CaCO 3 separated in the filter 8 is further used as described herein.
  • Fig. 2 shows a technical drawing of the reaction vessel 1 in cross section, wherein as a preferred variant, the Frings- Belüfitungsturbine is used.
  • Essential parts are the drive motor with extended shaft 12, which is performed by the elongated shaft directly driven rotor 4a, which is designed as a stirrer, the stator 4b, the intimately into the rotor 11 and intimately with the sucked from the feed line 3 gas in the rotor Form of a propulsion jet 13 radially ejected.
  • An inlet cylinder 14 directs the substantially reacted gas-liquid mixture in the direction of the suctioning rotor.
  • the reacted gas passes under slight overpressure in the next treatment station to remove the water vapor still contained in the gas.
  • the method practicable with this specific arrangement is virtually identical to the method described herein and in particular to the method described in connection with FIG.
  • FIG. 3 shows a diagram of an exemplary overall system for operating the reaction vessels required for carrying out the method according to the invention in the case of a batchwise operation.
  • the burnt lime (CaO) passes via an input line or input device 16 into the extinguishing reactor 17, which is connected to the Original liquid is substantially water-filled.
  • the finished solution is conveyed into the carboxylation reactor 1.
  • the contents of the reactor 1 are fed to a filter unit or separator 8.
  • the Trubfr quasi is supplied by means of an eccentric screw pump to a receiving vessel 18 with digestate, mixed with these and then decanted by means of a decanter 19.
  • the concentrated phase is low in water and represents the high-quality fertilizer 20.
  • Input volumetric flow of biogas about 2000 to 2200 m 3 per h, temperature about 20 to 45 ° C, inlet pressure about 0 to 20 mbar, Composition of the biogas itself as already indicated elsewhere for the untreated biogas, preferably about 60% methane, 37 to 40% CO 2 , 0.1% H 2 S, traces of O 2 and N 2 .
  • Operation sets a constant exhaust gas temperature, in discontinuous operation, this increases up to 80 ° C,
  • Methane content about 90 to 95%
  • the reaction is complete, with about 1520 kg CO 2 absorbed and converted to about 3117 kg CaCO 3 , the H 2 S completely converted to about 4.7 kg CaS and leaving the reactor biogas is free of siloxanes and has a CO 2 - residual content of about 5%.
  • the second reactor which is loaded with CaO or Ca (OH) 2 , the CO 2 content is less than 3%.
  • the CaCO 3 -containing solution in this example about 10 m 3 solution, is removed from the reactor, decanted after sedimentation, and mixed with one to three volumes of previously intensively aerated, then concentrated by a combination of mechanical and dynamic decanter concentrated digestate.
  • the fermentation residue comes from the processes of the methane reactors and that part which is enriched in microorganisms and Inertmasse / Inertschlamm, as well as the concentrates from microfiltration and reverse osmosis, and continue to share the unprocessed Dickschlempe.
  • the digestate contains about 14% TS, is mixed with the CaCO 3 obtained as described above and then dehydrated by means of eg a Karnmerf ⁇ lterpresse.
  • the remaining filter cake has a dry matter content of about 40%, is well storable and transportable, and represents a high quality fertilizer.
  • Input volume flow of biogas about 90 to 100 m 3 per h
  • Inlet pressure of the delivered biogas after leaving the compressor station about 200 mbar.
  • the CaCO 3 -containing solution is decanted in this case after sedimentation, filtered and predried to about 10% residual moisture in a heating oven at 105 ° Ceslius. Subsequently, the gromige powder is dried at about 800 ° C in a fluidized bed oven to completion and completely converted to CaO and a small amount of CaSO4.
  • the CaO is converted into Ca (OH) 2 in a quenching drum by the controlled addition of water.
  • the forming in this reaction exothermic heat is largely recovered by means of heat exchangers and utilized for the production of warm water.
  • the regenerated Ca (OH) 2 is reused to absorb further CO 2 from biogas.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Zoology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Biotechnology (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Biochemistry (AREA)
  • Microbiology (AREA)
  • Genetics & Genomics (AREA)
  • Molecular Biology (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Sustainable Development (AREA)
  • Fertilizers (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

La présente invention concerne un procédé de purification de biogaz qui consiste a) à préparer un biogaz, puis b) à faire passer le biogaz à travers un liquide d'appauvrissement qui appauvrit le biogaz en CO2 et/ou en H2S. Cette invention est caractérisée en ce que le liquide d'appauvrissement comprend Ca(OH)2.
PCT/EP2008/003286 2007-04-23 2008-04-23 Procédé de purification de biogaz et biogaz pouvant être ainsi préparé WO2008128776A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP08749085A EP2139831A2 (fr) 2007-04-23 2008-04-23 Procede de purification de biogaz et biogaz pouvant etre ainsi prepare

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007019118 2007-04-23
DE102007019118.0 2007-04-23

Publications (2)

Publication Number Publication Date
WO2008128776A2 true WO2008128776A2 (fr) 2008-10-30
WO2008128776A3 WO2008128776A3 (fr) 2009-01-15

Family

ID=39671373

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2008/003286 WO2008128776A2 (fr) 2007-04-23 2008-04-23 Procédé de purification de biogaz et biogaz pouvant être ainsi préparé

Country Status (2)

Country Link
EP (1) EP2139831A2 (fr)
WO (1) WO2008128776A2 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101993813A (zh) * 2009-08-18 2011-03-30 包德圻 利用废生物实现能源沼气化
EP2316917A1 (fr) 2009-11-03 2011-05-04 HF Biotec Berlin GmbH Procédé de culture de mixotrophes de microorganismes et/ou de cellules
CN102382698A (zh) * 2011-04-29 2012-03-21 王嘉兴 一种沼气净化副产碳酸钙的方法
EP2599750A1 (fr) 2011-11-29 2013-06-05 HF Biotec Berlin GmbH Procédé et installation de fabrication semi-continue de carbonate de calcium cristallin
EP2786967A1 (fr) * 2013-04-03 2014-10-08 HF Biotec Berlin GmbH Procédé et installation de fabrication de carbonate de calcium cristallin en utilisant deux gaz combinés ayant une teneur en CO2 différente
WO2017093701A1 (fr) * 2015-12-04 2017-06-08 Engie Dispositif et procédé de décarbonatation de biogaz

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1232129B1 (fr) * 1999-11-23 2003-11-05 Norsk Hydro Asa Additif pour engrais comprenant du sulfate et du carbonate de magnesium et de calcium
FI118734B (fi) * 2002-05-31 2008-02-29 Preseco Oy Menetelmä eloperäisen materiaalin jäännöksen käsittelemiseksi
JP3939204B2 (ja) * 2002-06-12 2007-07-04 中外炉工業株式会社 有機性廃棄物の消化ガスからのメタンの分離回収方法
EP1572323A1 (fr) * 2002-12-18 2005-09-14 Bioscent Systeme et dispositif pour eliminer des substances indesirables contenues dans un flux gazeux
ITBO20030476A1 (it) * 2003-08-04 2005-02-05 Biolchim S P A Concime idrosolubile in polvere contenente fosforo (p2 o5) e calcio (cao) in rapporti diversi.

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101993813A (zh) * 2009-08-18 2011-03-30 包德圻 利用废生物实现能源沼气化
EP2316917A1 (fr) 2009-11-03 2011-05-04 HF Biotec Berlin GmbH Procédé de culture de mixotrophes de microorganismes et/ou de cellules
CN102382698A (zh) * 2011-04-29 2012-03-21 王嘉兴 一种沼气净化副产碳酸钙的方法
EP2599750A1 (fr) 2011-11-29 2013-06-05 HF Biotec Berlin GmbH Procédé et installation de fabrication semi-continue de carbonate de calcium cristallin
WO2013079436A1 (fr) 2011-11-29 2013-06-06 Hf Biotec Berlin Gmbh Procédé et installation pour la fabrication semi-continue de carbonate de calcium cristallin
EP2786967A1 (fr) * 2013-04-03 2014-10-08 HF Biotec Berlin GmbH Procédé et installation de fabrication de carbonate de calcium cristallin en utilisant deux gaz combinés ayant une teneur en CO2 différente
WO2014161758A3 (fr) * 2013-04-03 2014-12-31 Papierfabrik August Koehler Se Procédé et installation permettant de préparer du carbonate de calcium cristallin en combinant deux gaz à teneur en co2 différente
US10662546B2 (en) 2013-04-03 2020-05-26 Papierfabrik August Koehler Se Method and system for producing crystalline calcium carbonate by the combined use of two gases with different CO2 content
WO2017093701A1 (fr) * 2015-12-04 2017-06-08 Engie Dispositif et procédé de décarbonatation de biogaz
FR3044563A1 (fr) * 2015-12-04 2017-06-09 Engie Dispositif et procede de decarbonatation de biogaz

Also Published As

Publication number Publication date
WO2008128776A3 (fr) 2009-01-15
EP2139831A2 (fr) 2010-01-06

Similar Documents

Publication Publication Date Title
EP2464614B1 (fr) Procédé et dispositif de fabrication de particules de charbon enrichies avec des matières minérales
DE102008050349B4 (de) Verfahren zur Ausfällung von Phosphor aus phosphatbelastetem Abwasser
DE2952794C2 (de) Verfahren und Vorrichtung zur Aufbereitung organischer Abfallmassen mit hohem Gehalt an Stickstoffverbindungen
CA2346706C (fr) Procede et usine de traitement de dechets liquides organiques
DE102005055310B4 (de) Verfahren zur Aufbereitung von Gärresten
WO2008128776A2 (fr) Procédé de purification de biogaz et biogaz pouvant être ainsi préparé
EP2252553B1 (fr) Procédé et dispositif de traitement des eaux usées
WO2015004146A1 (fr) Procédé et installation pour le traitement de déchets organiques
JPS5940518B2 (ja) セルロ−ス含有廃棄物の嫌気性消化方法
EP2130893A2 (fr) Procédé de fabrication de charbon, notamment de boue de charbon
DE102011120888B3 (de) Verfahren und Vorrichtung zum Abbau von biogenem Material
DE102015203484B4 (de) Verfahren zur Schlammbehandlung und Schlammbehandlungsanlage
EP3087171A1 (fr) Procédé et dispositif de production de biogaz
DE102015002416A1 (de) Verfahren zur Abtrennung von Phosphor aus Klärschlamm
AU2014356279B2 (en) Method and device for treating an organic effluent
EP3356299B1 (fr) Système pour le traitement des résidues organiques avec un procédé de carbonisation hydrothermal
DE19502856A1 (de) Vorrichtung und Verfahren zur Verminderung der Schlammproduktion in Kläranlagen
EP3630705B1 (fr) Procédé de conversion de fumier de volaille
CN1513766A (zh) 常压盐溶液法制取α-半水脱硫石膏工艺
DE102014001912A1 (de) Verfahren zur stofflichen und energetischen Verwertung biogener Reststoffe von Anlagen zur Bioethanolgewinnung und Anordnung zur Durchführung des Verfahrens
EP1829829B1 (fr) Procédé de séparation de biomasse
DE3823950A1 (de) Verfahren zur reduktion bzw. entfernung von ammoniak und/oder sonstigen geruchsaktiven stoffen aus organisch belasteten abwaessern
DE19800224C1 (de) Vergärung von Klärschlamm und Bioabfällen
DE102007056916B4 (de) Anlage und Verfahren zur Herstellung von Biogas
DE102013007076B4 (de) Verfahren und Anlage zur Gewinnung von konzentriertem, mineralischem Dünger aus Ausgangsstoffen mit organischem Anteil

Legal Events

Date Code Title Description
DPE2 Request for preliminary examination filed before expiration of 19th month from priority date (pct application filed from 20040101)
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08749085

Country of ref document: EP

Kind code of ref document: A2

WWE Wipo information: entry into national phase

Ref document number: 2008749085

Country of ref document: EP

NENP Non-entry into the national phase

Ref country code: DE