WO2020239878A1 - Procédé de production de biogaz - Google Patents

Procédé de production de biogaz Download PDF

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Publication number
WO2020239878A1
WO2020239878A1 PCT/EP2020/064775 EP2020064775W WO2020239878A1 WO 2020239878 A1 WO2020239878 A1 WO 2020239878A1 EP 2020064775 W EP2020064775 W EP 2020064775W WO 2020239878 A1 WO2020239878 A1 WO 2020239878A1
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WIPO (PCT)
Prior art keywords
digestate
liquid
aerated
liquid digestate
slurry
Prior art date
Application number
PCT/EP2020/064775
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English (en)
Inventor
Erik Nordell
Sandra WAERN
Jan Moestedt
Original Assignee
Tekniska Verken I Linköping Ab (Publ)
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 Tekniska Verken I Linköping Ab (Publ) filed Critical Tekniska Verken I Linköping Ab (Publ)
Priority to US17/614,106 priority Critical patent/US20220307058A1/en
Priority to EP20732123.3A priority patent/EP3976807A1/fr
Priority to CN202080039477.4A priority patent/CN114207138A/zh
Publication of WO2020239878A1 publication Critical patent/WO2020239878A1/fr

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Classifications

    • 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
    • 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
    • C12M1/00—Apparatus for enzymology or microbiology
    • C12M1/107—Apparatus for enzymology or microbiology with means for collecting fermentation gases, e.g. methane
    • 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
    • C12M1/00—Apparatus for enzymology or microbiology
    • C12M1/16—Apparatus for enzymology or microbiology containing, or adapted to contain, solid media
    • 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
    • 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

Definitions

  • the present document relates a method for production of biogas by adding a liquid digestate to the process.
  • One problem associated with food or organic waste from mainly households is that it may also contain different types of impurities, such as plastic, metal, glass and textiles.
  • impurities including the plastic bags or containers used to collect and contain the organic waste, must be removed before the waste can be digested. This is done through a pre-treatment of the waste, usually performed in several steps, before a so called slurry is obtained, which forms the base material for the digestion process.
  • the food or organic waste in a container or bag usually has a dry matter content of about 30-35% (i.e. 65-70% is water). After processing of the organic waste, the slurry usually has a dry matter content of around 8-19.9% (i.e.
  • a dilution fluid made up of water (mainly freshwater/tap-water) and different types of diluted liquids, such as for instance washing water from the dairy industry, milk, or other such fluids, are used for this process.
  • the retention time in the digestion chamber i.e. the time that the material is in the chamber
  • this leads to a decreased time for the slurry to be digested.
  • grit and gravel need to be removed from a substrate such as processed food waste (slurry) or other pumpable waste.
  • a substrate such as processed food waste (slurry) or other pumpable waste.
  • the most common way to remove inert particles from the substrate is by the use of a hydro-cyclone that amplifies the gravidity of the heavy particles, which then can be separated from the organic waste.
  • the main disadvantages with this method is that the cyclone requires water to work. This is both costly as well as negative for the bio-fertilizer quality due to dilution. In addition it shortens the retention time of the substrate in the upcoming digester. Summary
  • a method for producing biogas in an anaerobic digestion chamber from an un-treated organic substrate wherein said un-treated organic substrate has a dry matter of content of in the range of 20 to 90 % of total solids, wherein the method comprises the steps of:
  • un-treated organic substrate is meant a material which is delivered from a source, the organic material may comprise different types of waste, usually food waste from households, food waste from industries, food waste from stores, slaughterhouse waste or other types of industrially produced organic waste materials, such as fodder and silage.
  • the organic substrate may also be different types of crops used for production of biogas.
  • dilution fluid is meant conventional dilution fluids used for biogas production, such as freshwater, washing fluids from the dairy industry etc.
  • liquid digestate is meant a material which is taken from the digestion chamber and brought back into the pre-treatment step.
  • biogas is meant a mixture of gases produced by the digestion of the organic substrate in the absence of oxygen. The biogases thus include primarily methane and carbon dioxide, and they are most often used for fuel or for conversion to heat or electricity.
  • the digestate is the material which is left after the digestion process of the slurry containing the organic waste has been carried out.
  • the digestate is also considered as a bio-fertilizer, which is brought back to agricultural land, depending on the type of the organic waste used in the process.
  • the amount of bio-fertilizer is reduced, with an increased concentration of nutrients, such as nitrogen and phosphorus as additional effect. This reduces the transportation cost and increases the value of the bio-fertilizer (per volume unit).
  • the water consumption in the biogas production process can be reduced, which also has a positive impact on the environment.
  • the retention time of the digestate is increased, which increases the degree of degradation of the slurry.
  • the liquid digestate may be either an unaerated or aerated liquid digestate.
  • liquid digestate may be an
  • the method further comprises aerating said liquid digestate in an aeration chamber prior to the introduction into the pre treatment step where the digestate is aerated with any one of the gases selected from air, oxygen and nitrogen with a flow in the range of 0.1 to 100 m 3 gas/m 3 liquid h.
  • the liquid digestate is an aerated digestate and wherein the method comprises aerating said liquid digestate prior to the introduction into the pre-treatment step during a time period of at least 1 hour.
  • the retention time in the aeration chamber is longer than 1 hour, conventionally between 1 and 24 hours.
  • the viscosity of the aerated liquid digestate is decreased compared to untreated digestate during the aeration step as measured in cP.
  • the decrease of total amount of bio-fertilizer may be up to around 20-25%, which means that the nutrients, such as ammonium nitrogen, is accumulated in the digestion chamber, resulting in an increase of the nutrients by around 20%.
  • the liquid digestate replaces at least 5 % of the dilution fluid compared to conventional methods, or at least 25 % of dilution fluid, or at least 50 % of dilution fluid.
  • an additive for use in the method according to the first aspect, wherein said additive comprises an aerated liquid digestate from a digestion chamber.
  • the aerated liquid digestate has a viscosity as measured in cP which is lower than an untreated liquid digestate.
  • a method of cleaning an un-treated organic waste substrate prior to introduction into a biogas production facility wherein the cleaning is performed in a hydro-cyclone, and wherein said hydro-cyclone a cleaning liquid is used, wherein said cleaning liquid is at least partially composed of a liquid digestate from a digestion chamber.
  • liquid digestate may be any liquid digestate
  • liquid digestate is an aerated liquid digestate that has been treated in an aeration chamber.
  • Said aerated liquid digestate has a viscosity as measured in cP which is lower than an unaerated liquid digestate.
  • Fig. 1 is a schematic view of a biogas production process according to the inventive idea.
  • Fig. 2 is a graph showing the viscosity of aerated and unaerated digestate.
  • Fig. 3 is a graph showing a result of a pre-hydrolysis trial.
  • Fig. 4 is a graph showing a result of the gas composition from trials.
  • Fig. 5 is a graph showing hydrogen sulfide content in the off-gases from the pre-hydrolysis step (storage of slurry).
  • Fig. 6 is a graph showing the specific gas production in the continuous trail.
  • Fig. 7 is a graph showing the amount of ammonium nitrogen in the digestion chamber.
  • Fig. 8 is a graph showing pH and alkalinity.
  • Fig. 9 is a graph showing the principle for the hydro-cyclone with water and/or aerated digestate as a liquid additive.
  • Fig 1 illustrate an overview of the process.
  • a conventional biogas production organic waste material such as food waste, industrial waste etc. is brought into a pre-treatment tank 1 , here the waste material is pre-treated and thus mixed with dilution liquids, such as water (freshwater), or liquids from dairy or juice industry.
  • dilution liquids such as water (freshwater), or liquids from dairy or juice industry.
  • a facility such as the one at the Linkoping municipal biogas plant about 45 000-50 000 metric tons of liquids are used annually.
  • the slurry After the pre-treatment of the food waste, forming a slurry, the slurry usually has a dry substance content of 12-19.9 %, i.e. a slurry material.
  • the pre treated waste is usually brought to a second step in the pre-treatment, which is at least one pasteurization chamber 1 or 2 or pre-hydrolysis chamber (storage tank for processed organic waste, slurry), wherein the pasteurization chamber 2 pathogenic microorganisms are reduced or killed. Flere a certain degree of pre-hydrolysis occurs.
  • the waste slurry material is brought to digestion chamber 3, where the waste slurry material is continuously digested under anaerobic conditions to form the gases called biogas, i.e. methane, carbon dioxide etc.
  • the residue after digestion is called a digestate, and usually has a dry content of 3-9 %.
  • the digestate is used as a bio-fertilizer and is brought to the farmers in closed tanks, or to a treatment facility to increase the dry content. From a facility as the municipal biogas plant in Linkoping, Sweden, approximately 80 000 - 120 000 metric tons of bio-fertilizer is produced annually, this bio-fertilizer usually has an ammonium nitrogen content of 3,000-4,000 mg/L. The farmer normally wants as high ammonium nitrogen and phosphorus content as possible. Also, the large volume of digestate to transport to the farmers is associated with a high cost.
  • a portion of the liquid digestate is brought from a digestion chamber 3 to the pre-treatment chamber 1 to replace some of the dilution liquids conventionally used in this pre-treatment step.
  • pre treatment step is meant the step in the biogas process where the substrate material, i.e. undigested organic waste material of different origin is treated before it is brought to the digestion chamber.
  • a digestate from a digester chamber normally has a total solid (TS) content of 3-9% depending of the ingoing substrate and the degree of degradation of the material inside the digester. Moreover, the ammonium content varies depending of the substrate type, but if food waste is the main substrate the ammonium content typically is in the range of 2,000 to 4,000 mg/L (express as ammonium nitrogen).
  • a portion, or all, of the digestate is brought to an aeration chamber or tank 4.
  • air is provided to flow through the digestate, thereby forming a liquid aerated digestate material.
  • the liquid aerated digestate material has a lower dry content compared to the untreated digestate, normally in the range of 2-8 % based on total solids.
  • Fig. 1 it is shown that all of the liquid digestate removed from the digestion chamber is brought to and aerated in the reaction chamber, however it is sufficient that only the portion needed to for dilution in the pre-treatment chamber is aerated.
  • the aeration may be performed, but not limited to, aeration with air, pure oxygen, and mixture of oxygen/nitrogen.
  • the gas used in the reaction chamber comprises in the range of 1 to 100 % O2.
  • the flow of air in the reaction chamber is in the range of 0.1 to 100 m 3 gas/m 3 liquid and hour, more preferably 0.2 to 50 m 3 gas/m 3 liquid and hour and even more preferable 0.5 to 5 m 3 gas/m 3 liquid and hour.
  • the retention time of the liquid digestate in the aeration chamber is in the range of 1 to 500 hours, more preferably 2 to 100 hours and even more preferable 12 to 48 hours. In one embodiment the retention time is at least 1 hours, or at least 2 hours.
  • the viscosity of the aerated liquid digestate material has been reduced by at least 1 %, more preferably by 10% and even more preferable by 25% compared to the untreated, i.e. not aerated liquid digestate material.
  • This reduction of viscosity may be essential for the slurry produced in the pre-treatment step as it must have a certain viscosity for it to be fed in the system.
  • liquid digestate material around 50 % of the dilution liquids can be replaced by the liquid digestate material, both untreated and treated.
  • an aerated liquid digestate is used.
  • a replacement of around 50% of the dilution liquids leads to a reduction of the total amount of bio-fertilizer by around 20-25 % (under the conditions as set out in the municipal biogas facility in Linkoping, Sweden).
  • the water consumption decreases as well as the need for transportation of bio fertilizer from the site to farmers land, thus providing a substantial economical saving.
  • the first trial set was aimed at simulating a semi-continuously fed storage tank for food waste, food waste and liquid digestate and food waste and aerate liquid digestate - naturally a pre-hydrolysis (controlled or uncontrolled) occurred when storing the slurry.
  • a pre-hydrolysis controlled or uncontrolled
  • the pre-hydrolysis reactors operated at a temperature of 55 °C.
  • the liquid digestate which is provided in the aeration chamber has a significantly lower viscosity than untreated digestate.
  • shear rate 50 (s 1 ) in this example the viscosity drops from 41 cP down to 14 cP, a decrease with 66% compared to untreated digestate.
  • Aeration of the liquid digestate results in a substantial decrease in viscosity of the liquid digestate.
  • the digesters were operated at a temperature of 42 °C.
  • the retention time was determined to 35 days in the digestion step and three (3) days in the pre hydrolysis step (storage tank), i.e. approximately the same as in the pre hydrolysis trial.
  • the organic loading rate in the digesters were 4.0-4.5 kg VS/m 3 day during the experiment.
  • the first 30 days were used as start-up period were both reactors received the same slurry (food waste, milk, water).
  • the pre-hydrolysis reactors were fed daily with a mixture of food waste, water, milk, digestate or aerated digestate (see Table 1 ). And subsequently the slurry from those were fed into the digesters, one digester fed with slurry formed from food waste, water and milk; and another reactor fed with slurry formed from food waste, digestate (or aerated digestate), water and milk.
  • a comparative trial between using an untreated and aerated liquid digestate is provided in Figs 6 to 8.
  • Fig 7. shows the ammonium nitrogen content of the digestate from the two digesters fed with different slurries.
  • the reactor fed with slurry produced from the aerated digestate-mixture has a steady higher ammonium nitrogen content than the control.
  • the increase in ammonium nitrogen is 800 mg/L.
  • grit, gravel, glass etc. and heavy inert particles need to be removed from a substrate such as processed food waste (slurry) or another pumpable waste or material.
  • a substrate such as processed food waste (slurry) or another pumpable waste or material.
  • the most common way to perform this is by use a hydro-cyclone that amplifies the gravidity of the heavy particles, which then can be separated from the organic waste.
  • a cyclone is mounted in the circulation of the storage tank for processed food waste, the slurry.
  • the slurry has a TS content of 14-16% in normal case.
  • On an annual basis around 90 000 tons of slurry will pass the process.
  • the cyclones use around 10-15 L water/min to work, resulting in 5,000 m 3 water per year in consumption.
  • the dilution of the slurry is at this plant 5-6% due to the extra water added in this step, to separate heavy inert particles such as (but not limited to) grit and gravel from the organic slurry.
  • the high water consumption is both a cost and dilutes the bio-fertilizer as well as shortened the retention time of the substrate in the upcoming digester.
  • aerated digestate and thus a liquid with low viscosity
  • the water consumption may be cut with 1 -100% compared to the common used technique with water.
  • the aerated digestate is mixed-in to a substrate flow where the grit should be separated, there is of greatest importance to avoid gas bubbles and gas formation. Since the aerated digestate lacks dissolved methane and has low content of carbon dioxide this is a suitable liquid.
  • the aerated digestate has a low viscosity, which is a requirement to be able to use the digestate as a counter flow in the cyclone.
  • dilution can be avoided as the aerated digestate contains high amount of nitrogen and phosphorus etc. which is desirable in the bio-fertilizer. Even more positively, this cuts the amount of transports needed to transport the bio-fertilizer to the farmers at the end of the process. See Figure 9.

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  • Chemical & Material Sciences (AREA)
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  • Life Sciences & Earth Sciences (AREA)
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Abstract

Procédé de production de biogaz dans une chambre de digestion anaérobie à partir d'un substrat organique non traité, ledit substrat organique non traité ayant une matière sèche de teneur allant de 20 à 90 % de solides totaux, le procédé consistant à pré-traiter le substrat organique non traité, pour former une bouillie ayant une teneur en matière sèche comprise dans la plage de 8 à 19,9 % de solides totaux, à introduire ladite bouillie dans une chambre de digestion, à digérer ladite bouillie dans la chambre de digestion pour produire du biogaz et un digestat, dans ladite étape de prétraitement, un mélange d'un fluide de dilution et d'un digestat liquide provenant de ladite chambre de digestion étant utilisé pour diluer le substrat organique non traité.
PCT/EP2020/064775 2019-05-28 2020-05-27 Procédé de production de biogaz WO2020239878A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
US17/614,106 US20220307058A1 (en) 2019-05-28 2020-05-27 Method for the production of biogas
EP20732123.3A EP3976807A1 (fr) 2019-05-28 2020-05-27 Procédé de production de biogaz
CN202080039477.4A CN114207138A (zh) 2019-05-28 2020-05-27 用于生产沼气的方法

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SE1950637A SE543955C2 (en) 2019-05-28 2019-05-28 Method for the production of biogas
SE2050149-0 2019-05-28
SE1950637-7 2019-05-28

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Citations (6)

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US20070141691A1 (en) * 2005-12-19 2007-06-21 Stanley Consultants, Inc. Process for producing ethanol and for energy recovery
SE1150954A1 (sv) 2011-10-14 2013-04-15 Tekniska Verken Linkoeping Ab Biogasproducerande laboratoriereaktor
WO2014076483A2 (fr) * 2012-11-16 2014-05-22 Blaygow Limited Traitement de grains
WO2016066752A1 (fr) * 2014-10-29 2016-05-06 Cambi Technology As Procédé et dispositif pour le traitement de biomasse et de déchets organiques
EP3181524A1 (fr) * 2015-12-15 2017-06-21 André Holzer Procede et installation pour le traitement sous pression de charge liquide
US20180141841A1 (en) * 2015-06-12 2018-05-24 Sbm Developpement Novel solid-state anaerobic digestion method

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SE0202428L (sv) * 2002-08-14 2004-01-27 Tekniska Verken Linkoeping Ab Sätt och anordning för framställning av biogas
SE533193C2 (sv) * 2009-03-25 2010-07-20 Scandinavian Biogas Fuels Ab Biogasproducerande system
US10005995B2 (en) * 2012-08-29 2018-06-26 Renewable Energy Alternatives, Llc System and method for thermophilic anaerobic digester process

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US20070141691A1 (en) * 2005-12-19 2007-06-21 Stanley Consultants, Inc. Process for producing ethanol and for energy recovery
SE1150954A1 (sv) 2011-10-14 2013-04-15 Tekniska Verken Linkoeping Ab Biogasproducerande laboratoriereaktor
WO2014076483A2 (fr) * 2012-11-16 2014-05-22 Blaygow Limited Traitement de grains
WO2016066752A1 (fr) * 2014-10-29 2016-05-06 Cambi Technology As Procédé et dispositif pour le traitement de biomasse et de déchets organiques
US20180141841A1 (en) * 2015-06-12 2018-05-24 Sbm Developpement Novel solid-state anaerobic digestion method
EP3181524A1 (fr) * 2015-12-15 2017-06-21 André Holzer Procede et installation pour le traitement sous pression de charge liquide

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BANGXI ZHANG ET AL: "Effect of inoculated and uninoculated aeration pretreatment on nutrients and phytotoxicity of anaerobic digestion effluent", SCIENTIFIC REPORTS, vol. 8, no. 1, 17 September 2018 (2018-09-17), pages 1 - 8, XP055720618, DOI: 10.1038/s41598-018-32141-7 *
BAYO JAVIER ET AL: "Hydrocyclone as a cleaning device for anaerobic sludge digesters in a wastewater treatment plant", JOURNAL OF CLEANER PRODUCTION, ELSEVIER, AMSTERDAM, NL, vol. 87, 4 November 2014 (2014-11-04), pages 550 - 557, XP029101793, ISSN: 0959-6526, DOI: 10.1016/J.JCLEPRO.2014.10.064 *
S. VERMA: "ANAEROBIC DIGESTION OF BIODEGRADABLE ORGANICS IN MUNICIPAL SOLID WASTES Submitted in partial fulfillment of the requirements for Master of Science Degree in Earth Resources Engineering", COLUMBIA UNIVERSITY. SUBMITTED IN PARTIAL FULFILLMENT OF THE REQUIREMENTS FOR MASTER OF SCIENCE DEGREE IN EARTH RESOURCES ENGINEERING, 31 May 2002 (2002-05-31), pages 48, XP055247017, Retrieved from the Internet <URL:http://www.compost.org/CCC_Science_Web_Site/pdf/Biogas/anaerobic Digestion of Biodegradable Organics in MSW.pdf> [retrieved on 20160202] *

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