WO2012152266A2 - Procédé de production de biogaz à partir d'excréments essentiellement animaux - Google Patents

Procédé de production de biogaz à partir d'excréments essentiellement animaux Download PDF

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Publication number
WO2012152266A2
WO2012152266A2 PCT/DE2012/100124 DE2012100124W WO2012152266A2 WO 2012152266 A2 WO2012152266 A2 WO 2012152266A2 DE 2012100124 W DE2012100124 W DE 2012100124W WO 2012152266 A2 WO2012152266 A2 WO 2012152266A2
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Prior art keywords
fermentation
fermenter
biogas
substrate
ammonia
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PCT/DE2012/100124
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German (de)
English (en)
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WO2012152266A3 (fr
Inventor
Lothar Günther
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Dge Dr.-Ing. Günther Engineering Gmbh
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Priority to EP12730780.9A priority Critical patent/EP2707491A2/fr
Publication of WO2012152266A2 publication Critical patent/WO2012152266A2/fr
Publication of WO2012152266A3 publication Critical patent/WO2012152266A3/fr

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    • 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
    • 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
    • C02F11/02—Biological treatment
    • C02F11/04—Anaerobic treatment; Production of methane by such processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/20—Sludge processing

Definitions

  • the invention relates to a process for the production of biogas from predominantly animal excreta, in particular manure or chicken manure, individually or as a mixture, by a multi-stage anaerobic reaction in one or more fermenters.
  • biogas is carried out in a conventional manner in one or more reactors or fermenters that can be operated mesophilic (temperatures below 45 ' ⁇ ) or thermophilic (temperatures 45 to 80' ⁇ ).
  • biomass organic materials are used, for example, as farmyard manure, renewable resources and biological waste materials incurred. Sewage sludge is only suitable for anaerobic conversion if it is obtained from organically polluted wastewater or process water with a COD content of more than 5,000 mg / l, and thus is anaerobically convertible biomass.
  • COD is the abbreviation for "Chemical Oxygen Demand, which uses a COD measurement to determine how much oxygen the chemical digestion / purification processes in wastewater consume.
  • various biodegradation processes take place during the reaction, such as hydrolysis, acidification, acetic acid formation and methane formation.
  • the decomposition processes caused by bacteria can take place under aerobic or anaerobic conditions. The most commonly used method is wet fermentation where the dry matter content TS is ⁇ 15% and the water content is> 85%.
  • biogas with a methane content of up to 65% can be achieved in practice.
  • Biogas is used inter alia for heating purposes, e.g. used in combined heat and power plants, or as an energy source for feeding into natural gas networks.
  • the CO 2 contained in the biogas still has to be separated in order to obtain a high quality methane gas suitable for further processing.
  • the purification or processing of biogas is a technologically complicated process, which is associated with a high expenditure on apparatus.
  • animal excreta can not be anaerobically fermented according to the same procedure as other biomass substrates.
  • One problem is the relatively high level of ammonia in such substrates. Since, as is known, ammonia / ammonia compounds are additionally formed during fermentation, their rate of formation of methane is considerably impaired.
  • DD 217 786 A1 a method for the production of biogas from manure is known, manure is fermented in two stages successively under aerobic and anaerobic conditions.
  • DD 264 910 A1 Also known (DD 264 910 A1) is a process for obtaining biogas from pig manure, chicken manure, bovine manure or the like, with increased biogas production rate and biogas yield by a special material guide in the reactor.
  • a method is known from DE 3 843 789 A1, according to which fresh manure is first introduced into a hydrolysis reactor and stored in order to remove CO 2 and H 2 S and then the manure is fed to a solids separation and subsequent fixed-bed flow reactor in order to remove methane gas.
  • manure is first to be separated into a solid and liquid phase in order to produce biogas from the solid phase.
  • the invention has for its object to provide a method for the production of biogas from predominantly animal excrement, which is characterized by a higher yield of raw or biogas and a higher content of methane in the raw gas and enables an economically improved operation. Furthermore, the produced biogas should have a very low content of nitrogen.
  • the starting substrate used can consist exclusively of animal excrements. However, the animal excrements can also be converted into biogas together with biomass of non-animal origin, such as, for example, renewable raw materials or biological waste materials, the quantitative proportion being less than 50%.
  • Fermentation substrate (starting substrate) with a TS content of less than 15% is mixed at least with supplied ammonia-reduced fermentation liquid, in an amount over which a loading in the range of 2 to 2.5 g NH 4 I or below in the fermentation substrate. If the supplied fermentation substrate (starting substrate) does not have the required DM content, it is adjusted by appropriate dilution or concentration.
  • TS content In the lower part of the TS content should be 1 to 6%.
  • the suspension is heated to a temperature of 65 to 90 ° C, which is maintained for a predetermined period of a few hours.
  • ammonia-reduced fermentation liquor which only has an ammonium content of less than 2000 mg / l.
  • the ammonia-reduced fermentation liquid may originate from the ongoing process, with a liquid fermentation substrate being removed from one of the fermenters or secondary fermenters and removed at temperatures of from 90 to 180 ° C., preferably to 150 ° C., and a pressure of at least 0.5 bar, preferably up to 2 bar, above the pressure of the corresponding boiling point of water is treated.
  • the thermal treatment duration of the fermentation substrate should be less than two hours.
  • the fermentation substrate used to produce the ammonia-reduced fermentation liquid can also come from another biogas production process, or possibly also the fermentation liquid.
  • the circled fermentation liquid is pumped in a loop through a first heat exchanger and heated to temperatures of up to 1 10 ' ⁇ and then fed to another, second heat exchanger and further heated in this up to a maximum of 180' ⁇ .
  • the stripped fermentation liquor is compressed to a pressure of 1.5 to 12 bar, preferably at least 0.5 bar, above the pressure of the corresponding boiling point of water.
  • the compressed hot fermentation substrate or fermentation liquid enters a closed container. In this, traces of H 2 S and water vapor are released by a relaxation or while maintaining the container internal pressure from the fermentation substrate C0 2 , ammonia and discharged as a gas mixture via a pressure-controlled exhaust pipe integrated into the container.
  • the ammonia-reduced fermentation liquid is removed via a line from the container and added after cooling to substrate temperature to the fermentation substrate to adjust the desired loading of NH 4 + .
  • a subset of ammonia-reduced fermentation substrate can be returned to the fermenter.
  • the elimination of a partial amount of fermentation liquid from the fermenter takes place only after reaching a limit value for the release of a methane formation inhibiting amount of ammonia.
  • the urea formed can be hydrolyzed again.
  • enzymes such as urease
  • the nitrogen content may be more than 2 vol .-% depending on the residence time of the fermentation substrate in the fermenter at ammonium loadings of more than 3 g / l in the fermentation substrate. As the ammonium content increases and the residence time increases, the proportion of nitrogen in the biogas formed also increases. In particular, then in the post-fermenter or in the subsequent fermentation fermentation with extremely high nitrogen contents of 5 to 20 vol .-% is expected.
  • ammonia-reduced fermentation liquor originating from another biogas production process e.g. in a parallel biogas plant for the fermentation of biomass on a vegetable basis.
  • fermentation liquor and / or solids separated from fermentation substrate may be added to the fermentation substrate in the further fermentation process.
  • the present after the addition of ammonia-reduced fermentation liquid fermenting substrate with a loading of about ⁇ 2.5 g of NH 4 7I is subjected to a first fermentation for a period of one to four days at a pH of less than 6.5, preferably 5 to 6, whereby hydrolysis and acidogenesis take place, whereby a utilizable weak gas is used as first biogas stream with up to 50% of the total proportion of C0 2 and the superfluous amount of H 2 S and a part of NH 3 arise. It is a so-called Hydrofermlab (process step a)).
  • the per se conventional single-stage fermentation process is separated into two stages, which are referred to as Hydroferm- and Methanofermface.
  • the fermented fermentation substrate is pumped into the first fermenter and in this during a residence time of 10 to 30 days for further fermentation at temperatures of 35 to 60 ' ⁇ and a pH of 7 to 8 subjected to another Acidogenese, acetogenesis and Methanogenesis take place while a second biogas with methane contents of 65 to 75 vol .-% and lower hydrogen sulfide content than the produced lean gas is formed.
  • This process step c) is referred to as Methanofermlab.
  • the methane content in the biogas obtained after process step c) is at least a factor of 2 higher than the methane content in the weak gas produced according to process step b).
  • fermented fermentation substrate is subjected to at least one further fermentation step with a residence time of 20 to 80 days.
  • the further fermentation can be carried out in one or more fermenters connected in series, wherein a retention time of 20 to 80 days is to be maintained in each fermenter or secondary fermenter. Each fermenter also produces a separate biogas stream.
  • the resulting fermentation substrate is separated into a liquid and a more viscous to solid phase.
  • the liquid phase should have a TS content of less than 5% and the thicker to solid phase a TS content of 20 to 30%.
  • the thicker to solid phase is pumped into the subsequent fermenter.
  • the liquid phase is fed in whole or in part to the starting substrate and / or fermentation substrate during one or both treatments according to process steps a) and b).
  • the liquid phase can be partially or completely fed to one of the upstream fermenters.
  • biogas produced in the methanoferm stage has low contents of H 2 S and NH 3 and is free of oxygen. This results in much lower Expenses for the subsequent purification of biogas, in particular for desulfurization.
  • the resulting fermentation residue has a considerably lower ammonia load, which is advantageous for the environment, in particular with regard to the occurrence of lower odor nuisance.
  • TOC organic dissolved carbon
  • the amount of solid arising after the fermentation stages can be divided, e.g. a subset is admixed to the starting substrate for adjusting the TS content and the other subset is fed to one of the fermenter or secondary fermenter.
  • the generated biogas streams are, either individually or merged into a total stream, subjected to further purification and treatment.
  • the first fermenter and the second fermenter or secondary fermenter are designed in their useful volumes so that a volume ratio of greater than 1: 1 to 4: 1 is present.
  • the secondary fermenter should therefore have a lower useful volume, preferably half of the first fermenter.
  • the volume of digestate used should be reduced continuously, starting from the first fermenter to the last fermenter or post-fermenter, by half to one tenth, preferably to one fifth.
  • the temperatures in the fermenters should either be kept at the same level or rise from fermenter to fermenter.
  • the ammonia-reduced fermentation liquor can be stored for a predetermined period of time before being fed to the fermentation substrate to improve the biology.
  • the first stage to adjust the TS content of manure, either a portion of liquid may be separated or a fermentation substrate derived from a subsequent stage may be added as a solid. In individual cases, this depends on the composition of the manure.
  • the procedure according to the invention enables a particularly economical utilization of animal excrements to biogas.
  • the claimed process stages a), b) and c) are separated for each starting substrate and carried out in parallel. After completion of process step c), the respectively angegorenen substrates are pumped for further common treatment in the first fermenter. All other process steps then continue, as previously described, from.
  • the advantage of this variant is a better economical utilization of the biogas plant under the aspect of a higher biogas yield with higher methane content and lower nitrogen contents.
  • the starting substrate used is 7000 m 3 of bovine manure per year.
  • the manure has the following composition:
  • the biogas plant consists of a two-stage fermentation substrate preparation unit B for manure or HTK, a fermenter F1, which is connected to a loop K for the elimination of liquid, already fermented fermentation substrate, which is returned after removal of ammonia in the second stage B2 of the fermentation substrate preparation unit B.
  • a separator R for the removal of ammonia is inserted into the circulation loop K. prevented.
  • the biogas plant also includes a second fermenter or secondary fermenter F2 and a digestate storage GRL1.
  • a single-stage fermentation substrate preparation unit HF can be integrated into the biogas plant in order to additionally produce biomass on a non-animal basis, such as e.g. Corn silage, with to process, as explained in Example 3.
  • the first stage B1 of the fermentation substrate preparation unit B for liquid manure is fed via line 1 continuously 1 m 3 / h of cattle manure.
  • a tube bundle heat exchanger W is included, in which the manure is preheated.
  • the fermentation substrate processing unit B is designed as a heatable container, which is subdivided into two chambers, as first stage B1 and second stage B2.
  • the slurry pumped into the first chamber B1 is heated to a temperature of 80 ° C. with gentle stirring. The heating takes place via an indirect heat transfer medium. The temperature is maintained for a period of about 2 hours. Hygienisation is carried out at this stage to ensure the required hygienic safety.
  • the manure passes into the second stage B2, in which the circulation loop K is incorporated for the recirculate.
  • ammonium content of fermented manure varies extremely strongly and is dependent on the urea, urine and uric acid contained in the manure, which are also subject to considerable fluctuations.
  • the removal of ammonia and recycling of the recirculate in the ongoing biogas process, the ammonium content in the fermenter can be selectively influenced in order to avoid exceeding critical conditions to inhibit methane formation.
  • the residence time of the mixture (pH 6) in the second container B2 is 4 days. Within this time, biology is building up and the first fermentation processes (hydroforming stage), which lead to methane gas production. Decisive for this is the reduction of the ammonia content in the supplied manure by mixing with liquid, ammonia-reduced fermentation substrate in the ratio 1: 3 and separated fermentation liquid, as explained above. This results in a total mixing ratio of 1: 4.
  • the loading of NH 4 I in the fermentation substrate is less than 2 g, for example 1 g.
  • liquid fermentation substrate which is obtained after the post-fermenter F2, via the lines 1 1 and 5 in the first stage or the first chamber B1 are introduced if the manure has too high a content of TS.
  • biogas Due to accelerated formation of biogas, biogas is already produced in the second stage or chamber B2 as a lean gas in an amount of 8.5 m 3 / h of the following dry composition:
  • the gas composition fluctuates because it is a dynamic process and the slurry composition is not constant.
  • the resulting first biogas stream is discharged via line 16 and is a non-combustible gas which is fed to a downstream first purification stage, are removed in the biologically hydrogen sulfide and remaining amounts of ammonia in a conventional manner.
  • the lean gas After leaving the first purification stage, the lean gas still has a content of H 2 S of 30 to 100 ppm and NH 3 of 20 to 60 ppm.
  • C0 2 is separated from the lean gas according to known per se procedure.
  • this biogas can either be supplied to a CHP for generating electric power or mixed with the second biogas stream, which is produced in the main fermenter F1 and is withdrawn via line 17. 7 kWh of electricity and 10.5 kWh of heat energy can be generated from the biogas produced in a quantity of 3.3 m 3 / h.
  • the residence time of the fermentation substrate mixture (pH 7.5) for further fermentation is about 12 days while maintaining a fermenter temperature of about 55 ' ⁇ .
  • the fermenter has a volume of 1500 m 3 .
  • residence time of Gärsubstratgemisches in the first fermenter F1 are continuously removed via the line 7 of the loop K 4 m 3 / h of liquid fermentation substrate and at a pressure of 3 bar and a temperature of 1 15 ° C in the separator R subjected to a combined separation of ammonia with simultaneous thermal digestion of bio-unreactable organic components of the liquid fermentation substrate. Due to the increase in temperature escape from the fermentation substrate C0 2 , NH 3 and small amounts of water vapor. In a closed system, a system pressure of 7.5 bar would occur at 1 15 ° C. Since this is limited to 3 bar, escape under these conditions, the separating from the fermentation substrate components C0 2 and ammonia as gas. Water would evaporate under these conditions at about 1, 8 bar.
  • urea or uric acid which accumulates during the fermentation process or may be formed from the ammonia during the fermentation process, it may be necessary to increase the working temperature in the circulation loop for the separation of ammonia to up to 180 °. Under these conditions, urea decomposes to ammonia and carbon dioxide, which are discharged with the gas stream. The residence time for the thermal decomposition of urea is sufficient for 30 minutes for the present conditions. This is particularly necessary if the liquid fermentation substrate is circulated over a very long period of many months.
  • ammonium / ammonia is removed via line 8 and converted to ammonium sulfate, which is used as fertilizer.
  • the ammonia-reduced fermentation liquor (4 m 3 / h) obtained after the above-mentioned treatment with a residual ammonia content of about 850 mg / l is, as already explained above, fed to the second stage B2 of the fermentation substrate preparation unit and the fermenter F1.
  • the remaining amount (about 1 m 3 / h) of fermented fermented substrate is discharged from the fermenter F1 and passed via line 9 in the second fermenter or post-fermenter F2, which has a volume of 1000 m 3 . In this case takes place at a residence time of about 40 days, a biological conversion of not yet fermented organic substance Biogas, whereby a third biogas stream is generated, which is fed via the line 18 into the conduit 17 for the second biogas stream.
  • the fermentation substrate is reduced to a TS content of 2.5 to 5%, an OTS of 68.5%, a TOC of 6540 mg / l and an ammonium content of 1, 52 g / l.
  • resulting fermentation residue is passed via line 10 to a separator D and separated into a liquid and a solid phase.
  • the liquid phase is divided as follows: a first subset is via the lines 1 1, 12 in the fermenter or post-fermenter F2, a second subset via the lines 1 1, 4 or 5 in the slurry processing B and the rest via the line first 1, 13 pumped into the digestate storage GRL1.
  • the proportion of water introduced with the starting substrate slurry can be compensated for by adding solid digestate from the fermentation residue storage to adjust the TS content of the liquid manure.
  • the required amount of solid (1 600 kg / d, TS content 28%) passes via the indicated transport path 15 in the second stage B2 of the fermentation substrate preparation unit B or can via the transport path 14 in the Grestrestlager GRL1.
  • digestate can also be added to the first fermenter F1 and / or second fermenter or post-fermenter F2 in order to change the TS content of the fermentation substrate.
  • the pumped into the fermentation residue GRL1 digestate (1 m 3 / h) has a dry matter content of 3% and is used for example as an agricultural fertilizer.
  • the advantage is the relatively low content of ammonium / ammonia, whereby the odor is significantly reduced.
  • the starting substrate used is a quantity of 500 kg of poultry dry manure (HTK) per day.
  • the HTK has the following composition:
  • the structure of the biogas plant is analogous to the plant described in Example 1. Only the size is adapted to the smaller amount of substrate. 500 kg of HTK are fed once a day to the first stage B1 of the fermentation substrate preparation unit B, which mixture is mixed with 1000 l of liquid fermentation substrate via the line 5 to form a suspension and adjusted to a TS content of 14%.
  • the HTK suspension is heated with gentle stirring to a temperature of 80 ' ⁇ . The temperature is maintained for a period of about 2 hours. At this stage, the HTK suspension is sanitized.
  • the HTK suspension is pumped into a second container B2 (second stage), in which the line 2 of the circulation loop K is integrated for the supply of ammonia-reduced fermentation substrate.
  • 1 m 3 / h liquid fermentation substrate are removed from the first fermenter F1, the main fermenter, subjected to ammonia removal and pumped into the second container B2.
  • the supplied ammonia-reduced fermentation substrate has a temperature of 50 ' ⁇ .
  • the residence time of the mixture in the second container B2 is 4 days, with a TS content of less than 5%.
  • the reaction volume of the second container B2 is about 80 m 3 .
  • biology builds up and already the first fermentation processes, which lead to a gas formation. Decisive for this is the lowering of the ammonia content in the liquid manure supplied by mixing with liquid, ammonia-reduced fermentation substrate in the ratio 1: 20.
  • biogas formation is accelerated and biogas is already produced in the second tank as a lean gas in an amount of 0.5 m 3 / h of the following dry composition:
  • the gas composition varies because the HTK composition is not constant. After completion of the residence time of the fermentation substrate mixture in the second stage B2 of the fermentation substrate preparation unit B, this is pumped into the fermenter F1 in an amount of 1250 l / h.
  • the residence time of the fermentation substrate mixture for fermentation is about 14 days while maintaining a fermenter temperature of about 55 ° C.
  • the fermenter has a volume of 500 m 3 .
  • the withdrawn biogas is purified and dried according to the desired quality in a conventional manner. Shortly before the end of the residence time of the fermentation substrate mixture in the fermenter, after about 12 to 13 days, 1, 5 m 3 / h of liquid fermentation substrate on the recirculation loop K are removed and subjected to ammonia removal under analogous conditions as in Example 1, with a residual content to ammonium of about 940 mg / l.
  • the post fermenter or fermenter F2 has a volume of 300 m 3 .
  • the residence time of the fermentation substrate in the post-fermenter F2 is 62 days. Under these conditions, a reduction of 60% of the organic dry matter contained in the fermentation substrate (oTS).
  • the resulting digestate can be used as agricultural fertilizer.
  • the separated liquid fermentation substrate is returned to the fermentation stages, tank B2, main fermenter F1 and post-fermenter F2, to adjust the required DM content.
  • tank B2 main fermenter F1 and post-fermenter F2
  • the operation of the biogas plant can thus be carried out without wastewater.
  • HTK biogas in a particularly economical mode of operation produces 5.1 m 3 / h of biogas with an average CH 4 content of 62% by volume.
  • the different starting substrates are treated separately, manure analogously as in Example 1.
  • the process steps a), b) and c) according to the invention, including the so-called hydroferm stage, are carried out separately for manure and corn silage.
  • the first fermenter F1 main fermenter
  • the different fermentation substrates are brought together into a mixture.
  • Plant technology, the biogas plant is compared to the above-described embodiment still extended to a single-stage fermentation substrate processing unit consisting of a fermenter HF with a metering screw 20 for feeding corn silage, a line 21 for the discharge of biogas and a line 22 for forwarding angegorenem substrate in the first fermenter F1 consists.
  • the fermenter (volume 300 m 3 ) is also in the existing piping system for supplying ammonia-reduced fermentation liquid via line 23 and separated fermentation liquid (in the separator D) via the lines 1 1, 24 integrated.
  • the starting substrate cattle slurry is treated analogously as in Example 1.
  • the fermentation tank HF is fed via a metering screw 20 corn silage (580 kg / h). 24 liquid fermentation substrate (5 m 3 / h) at a temperature of 40 to 55 ' ⁇ , at the same time via lines 1 1, supplied which is obtained after the solid-liquid separation in the separator D. Due to the elimination of fermentation liquid from the first fermenter F1 and the removal of ammonia, the proportion of ammonium / ammonia in the entire cycle of the biogas plant is reduced. In addition, ammonia-reduced liquid fermentation substrate can also be fed via line 23.
  • a non-flammable gas with a mean methane content of 16.4 m 3 / h is produced. This biogas stream is combined with the first biogas stream from the second stage of the fermentation substrate preparation B2 and purified.
  • a combustible biogas (34.8 m 3 / h) is produced with a share of 18.1 m 3 / h of methane.
  • This biogas has the following dry composition:
  • the residence time of the fermentation substrate mixture in the first fermenter F1 for further fermentation is about 12 days while maintaining a fermenter temperature of about 55 ' ⁇ .
  • the fermenter F1 has a volume of 3000 m 3 .
  • the resulting ammonia-reduced fermentation liquor (9 m 3 / h) with a residual ammonia content of about 820 mg / l is, as explained above, fed to the second stage B2 of the fermentation substrate preparation unit and / or the corn pretreatment (fermentor HF) and / or the fermenter F1 ,
  • the residual amount (about 1.5 m 3 / h) of fermented fermentation substrate is discharged from the fermenter F1 treated further, as described in Example 1 (separator D, second fermenter or post-fermenter F2, etc.).
  • the fermentation substrate is reduced to a TS content of 2.5 to 5%, an OTS of 68.5%, a TOC of 5840 mg / l, and the ammonium content is 1.35 g / l.
  • the digestate (1, 3 m 3 / h) pumped into the GRL1 digestate store has a TS content of 2.5 to 5% and is used, for example, as agricultural fertilizer.
  • the TOC content is lower by a factor of 2 to 4.

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Abstract

L'invention concerne un procédé de production de biogaz à partir d'excréments essentiellement animaux, notamment de lisier ou bien de matières fécales de volailles, tels quels ou sous forme de mélange. L'invention remédie aux inconvénients de l'état de la technique en créant un procédé qui se distingue par un rendement plus élevé en gaz brut ou biogaz ainsi que par une teneur plus élevée en méthane dans le gaz brut et en permettant un mode de fonctionnement amélioré plus économique. Le biogaz produit doit également présenter une très faible fraction d'azote. Le procédé selon l'invention comprend notamment les mesures consistant à : - mélanger le substrat de fermentation à au moins un liquide de fermentation ajouté à teneur réduite en ammoniaque, dans une quantité qui permet de régler une charge égale ou inférieure à 2,5 g NH47I dans le substrat de fermentation, - le substrat de fermentation obtenu est soumis, pendant 1 à 4 jours pour une valeur de pH inférieure à 6,5, à une première fermentation au cours de laquelle se produisent une hydrolyse et une acidogénèse, entraînant la production d'un gaz pauvre comme premier flux de biogaz, - le substrat de fermentation dont la fermentation est amorcée est ensuite pompé dans un fermenteur suivant dans lequel il est soumis à une autre fermentation, au cours de laquelle se produisent une autre acidogénèse, une acétogénèse et une méthanogénèse, entraînant la production d'un deuxième flux de biogaz ayant une teneur en acide sulfurique inférieure à celle du gaz pauvre.
PCT/DE2012/100124 2011-05-10 2012-05-04 Procédé de production de biogaz à partir d'excréments essentiellement animaux WO2012152266A2 (fr)

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CN103304123A (zh) * 2013-07-04 2013-09-18 哈尔滨瀚科环境工程设计研究院有限公司 一种利用余热生产沼气的热能再利用装置及其运行方式
EP2682378A3 (fr) * 2012-07-05 2015-10-14 Wolfgang Tentscher Dispositif et procédé destinés au traitement de biomasse contenant de l'azote
WO2016036339A1 (fr) 2014-09-05 2016-03-10 Llc Integro-Sd. Procédé et bioréacteur pour le traitement de fientes de volaille pour obtenir de l'engrais organique et du biogaz
WO2016059621A1 (fr) * 2014-10-17 2016-04-21 Massai Giordano S.R.L. Installation et procédé pour le traitement de fumier de volaille
WO2017080565A1 (fr) * 2015-11-15 2017-05-18 Xergi Nix Technology A/S Procédé de fermentation de litière de volaille et production de biogaz
EP3181524A1 (fr) 2015-12-15 2017-06-21 André Holzer Procede et installation pour le traitement sous pression de charge liquide
MD4472C1 (ro) * 2015-03-11 2017-10-31 Государственный Университет Молд0 Procedeu de obţinere anaerobă a biogazului
TWI709539B (zh) * 2019-11-19 2020-11-11 董舒麟 複式厭氧曳流生物反應系統

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DE102012211781A1 (de) * 2012-07-05 2014-01-09 Wolfgang Tentscher Verfahren zur Erzeugung von Biogas aus stickstoffhaltiger Biomasse, einschließlich Ammoniakfermentation und Biogasfermentation
RU2526993C1 (ru) * 2013-03-20 2014-08-27 Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Кемеровский государственный сельскохозяйственный институт" Способ получения биогаза из экскрементов животных
DE102013018833A1 (de) * 2013-11-10 2015-05-13 Binowa Gmbh Verfahren zur Aufbereitung eines aus einem Fermenterreaktor stammenden Reststoffes
CN107475303B (zh) * 2017-08-11 2021-08-24 金寨县峰远黑猪养殖专业合作社 一种安全环保沼气的制备方法

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EP2682378A3 (fr) * 2012-07-05 2015-10-14 Wolfgang Tentscher Dispositif et procédé destinés au traitement de biomasse contenant de l'azote
CN103304123A (zh) * 2013-07-04 2013-09-18 哈尔滨瀚科环境工程设计研究院有限公司 一种利用余热生产沼气的热能再利用装置及其运行方式
WO2016036339A1 (fr) 2014-09-05 2016-03-10 Llc Integro-Sd. Procédé et bioréacteur pour le traitement de fientes de volaille pour obtenir de l'engrais organique et du biogaz
WO2016059621A1 (fr) * 2014-10-17 2016-04-21 Massai Giordano S.R.L. Installation et procédé pour le traitement de fumier de volaille
MD4472C1 (ro) * 2015-03-11 2017-10-31 Государственный Университет Молд0 Procedeu de obţinere anaerobă a biogazului
WO2017080565A1 (fr) * 2015-11-15 2017-05-18 Xergi Nix Technology A/S Procédé de fermentation de litière de volaille et production de biogaz
EP3181524A1 (fr) 2015-12-15 2017-06-21 André Holzer Procede et installation pour le traitement sous pression de charge liquide
TWI709539B (zh) * 2019-11-19 2020-11-11 董舒麟 複式厭氧曳流生物反應系統

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