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
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F3/00—Biological treatment of water, waste water, or sewage
  • C02F3/28—Anaerobic digestion processes
  • C02F3/2833—Anaerobic digestion processes using fluidized bed reactors
• • 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
  • C12P7/00—Preparation of oxygen-containing organic compounds
  • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
  • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
  • C12P7/06—Ethanol, i.e. non-beverage
  • C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
  • C12P7/10—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/02—Treatment of water, waste water, or sewage by heating
  • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
  • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
• • 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
  • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
  • C02F2103/325—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from processes relating to the production of wine products
• • 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
  • Y02E50/10—Biofuels, e.g. bio-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
  • 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 invention relates to a methanation process from a liquid phase which is a co-product resulting from the extraction of a main product obtained from a vegetable raw material.
• the invention relates, for example, to a method of methanation from a product extracted from a fermented must, in particular from the vinasse resulting from the distillation of a fermented must of a vegetable raw material in the framework of the production of alcohol, from a vegetable raw material, especially starchy plants and / or sacchariferous plants and / or lignocellulosic plants.
• Such a process for producing alcohol is, for example, of the type that comprises the following steps:
• phase I ldique fermented must, for example in a distillation column, with recovery of the alcohol at the top of the column, vinasse at the bottom of the column.
• the method may also provide for recovery of the flegmasses obtained at the level of the rectification step.
• the liquid phase of the vinasse is a co-product of the production of alcohol that can be valorized, for example for the production of thermal and / or electrical energy, by subjecting it to an anaerobic digestion treatment.
• the technique used for separating the co-product in the liquid phase is such that the mass content of suspended solids in the liquid phase of the vinasse before methanation is less than 1%, especially 0, 25% and more particularly 0.2% or even more preferably of the order of 0.1% (analysis according to standard NF EN 872).
• the methanation according to the invention may also be applicable to the liquid-phase coproduct produced by the production of other products, for example the production of beer, cider, champagne or vinegar. , soy products, amino acids, citric acid, succinic acid and other acids, the production of yeasts, vitamins, antibiotics, sauerkraut, cheeses, fermentation from the vegetable raw material containing sweet principles, starchy principles and cellulosic principles.
• the methanation step is thus relatively long, and can last more than 30 days, which is extremely disadvantageous for a large-scale industrial treatment.
• the residual pollution of the effluents resulting from anaerobic digestion is important and the installation must be completed by an aerobic biological treatment stage leading to large reactor volumes and a significant biological sludge production.
• WILKEN ING also relates to a process for producing ethanol and methane from biomass.
• the duration of the anaerobic digestion step remains long.
• the WILKEN ING process refers to a content of 1% MES, it does not propose any industrial solution to achieve such a rate.
• tests carried out by the applicants have shown that the low yields obtained for anaerobic digestion do not make it possible to envisage a profitable industrial implementation, especially with regard to the durations necessary for anaerobic digestion.
• the purpose of the invention is in particular to reduce the time required for the methanation step and also to reduce the production of sludge, by offering recycling possibilities for the effluents resulting from anaerobic digestion, in particular in the form of water which may be particularly used in the production process of the main product and thus reduce the consumption of the water used for the production of the must.
• the invention proposes a methanation process, from a liquid phase which is a co-product resulting from the extraction of a main product obtained from a vegetable raw material, characterized in that the content mass of suspended solids (MES) in said liquid phase is less than 0.25%, and the methanization treatment of said liquid phase is carried out using a very high yield methanizer.
• MES suspended solids
• a very high yield methanizer it is a methanizer with a yield greater than 90%.
• the mass content of suspended solids (MES) in said liquid phase is less than 0.2%, especially less than or equal to 0.1%.
• the very high yield methanizer may comprise a bed of granular sludge, fluidized, recirculated or expanded in one or more stages or sludge flocculated in an upward flow of the liquid phase.
• the methanizer with very high efficiency can also be:
• the invention thus proposes a methanization process with a very high yield, from a liquid phase which is a co-product resulting from the extraction of a main product obtained from a vegetable raw material, the mass content of materials. in suspension (MES) in said liquid phase being less than 0.25%, advantageously less than 0.2%, especially less than or equal to 0.1%.
• MES mass content of materials. in suspension
• the removal efficiency of carbon pollution (COD and BOD 5 ) is of the order of 90% and up to about 97%.
• the very high yield obtained during the methanation makes it possible to eliminate almost all the soluble biodegradable pollution, which makes it possible to directly envisage a treatment by membrane devices, and in particular by the reverse osmosis technique.
• the methanation treatment is carried out according to a diet drawing of said liquid phase in a methanizer of the "Anapulse"type;
• the methanation treatment is carried out by means of a fluidized bed reactor of biomass in a methanizer of the "Anaflux" type;
• the methanation treatment is carried out by means of a fixed bed reactor of biomass in an "Anafiz" type anaeriser
• At least one effluent from the methanization is subjected to a stripping and decarbonation step, and in that at least a fraction of the decarbonated effluent obtained is recycled at the head of the methanization;
• said recycled fraction is between 0 and 400% by weight of vinasses and phlegmasses
• the fraction of the decarbonated effluent that is not recycled at the top of the methanation is subjected to filtration capable of stopping particles of dimensions of the order of 0.2 ⁇ m, in particular bacteria;
• said fraction of the decarbonated effluent is subjected to a biological treatment of the carbon and / or nitrogen pollution, and / or to a physicochemical treatment of the phosphorus pollution;
• reverse osmosis filtration produces a retentate which then undergoes a so-called evaporation-concentration step, and in that the condensates recovered after evaporation-concentration can be used in the form of 'water.
• FIG. 1 is a diagrammatic representation of the major main groups of operations that generally comprise a first example of a process for producing a main product and a phase-in-phase coproduct capable of being methanized. the separation of phase I iquid intervening before the extraction of the main product;
• FIG. 2 is a diagrammatic representation of the major main groups of operations generally included in a second example of a process for producing a main product and a phase-in-phase coproduct capable of being methanized, the separation of the phase Iiquid intervening after the extraction of the main product;
• FIG. 3, in the form of three consecutive and chained portions 3A, 3B and 3C, is a detailed representation of the main groups of operations included in an example of a method for producing a main product and a in the ionic phase, capable of being methanized, the separation of the active phase prior to the extraction of the main product, and the main groups of operations included in an example of a methan isation process; treatment of the methanization effluents in accordance with the teachings of the invention;
• FIG. 1 shows a process for obtaining a main product obtained upstream of the methanation.
• This is for example ethanol, bioethanol, etc.
• This process comprises, in particular, from the MPV, a wort preparation stage, a biological activity stage (for example a stage of transformation and production of the main product) and a stage of separation before extraction of the phases.
• the ide and soil ide The so-called separation step, whether before or after (see Figure 2) the extraction of the main product, leads to the production of two co-products.
• a main co-product or coproduc it i qu i is the phase liquid resulting from the separation step.
• a secondary co-product or coproduct 2 which is the solid phase resulting from the separation step.
• the separation technique for example according to the teachings of the aforementioned John MAHLER document, the main characteristic of co-product 1 (liquid phase) is its mass content of suspended solids ( MY)
• the solid phase separation (COPRODUIT 2) / liquid phase (COPRODUIT 1) is carried out under conditions such that the mass content of suspended solids (MES) in the liquid phase (COPRODUIT 1) before methanation is less than 0.25% and preferably less than 0.2%, especially less than or equal to 0.1%.
• Figures 1 and 2 are two schematic diagrams illustrating the two versions (before and after extraction) of the separation for the production of the main co-product or coproduct 1 which will then undergo the methanation process.
• FIG. 3 is a detailed overall representation which shows "upstream" and in more detail an example of the production by extraction of the main product and the separation of the two co-products in an example in which this separation takes place before extraction, that is to say corresponding to the schematic representation of FIG. 1.
• FIG. 3 shows "upstream" and in more detail an example of the production by extraction of the main product and the separation of the two co-products in an example in which this separation takes place before extraction, that is to say corresponding to the schematic representation of FIG. 1.
• MPV which is constituted by Cereals.
• the preparation of the wort indicated in FIG. 1 is detailed in FIG. 3 in the form of the cleaning-grinding stages of the cereals, the stirring by adding water, the liquefaction and soda enzymes, and the liquefaction by means of water vapor, and saccharification by adding acid, antiviscosity enzymes and saccharification enzymes.
• Liquefaction and saccharification are aimed at obtaining a fermentable sugar.
• the biological activity step which, for example, is a fermentation process by adding yeasts, salts, air and water.
• the separation of the phases I ld ide and sol ide includes a first step dite treatment (Mahler process) by adding products to modify pH and filter aids for example based on polymers, then a step of physical separation, by means of, for example, a filter press, of the two phases of the invention and solids, the separation being for example by filtration and pressing.
• a first step dite treatment Melt process
• a step of physical separation by means of, for example, a filter press
• the separation being for example by filtration and pressing.
• On the right-hand side of Figure 3A are indicated the various products and elements necessary for the various steps or sub-steps of wort preparation, development and production of the main product (biological activity) and separation.
• the liquid phase Downstream of the separation, and going to part 3B of FIG. 3, as a comment, in this particular example, the liquid phase is also called filtered fermented wine.
• the phase sol ide, or coprodu it 2 is also called
• This co-product 2 has for example a fuel use.
• coprodu it 2 Before being used as a fuel, the coprodu it 2 can be washed with hot wash water, this washing water of coprodu it 2 then being added to co-product 1 (Filtered Fermented Wine), and this before the extraction of the main product.
• co-product 1 Frtered Fermented Wine
• the main product can, according to a first option A, dehydration whose source of energy is for example steam under pressure, to produce bioethanol.
• the alcoholic phlegmasses resulting from the dehydration can be reintroduced upstream of the distillation.
• the main product resulting from the distillation undergoes a rectification, for example by means of steam under pressure, for the production of rectified alcohol.
• the methanation process mentioned in FIGS. 1 and 2 is, in a known manner, essentially constituted of a first step known as Acidogenesis, then of a second stage known as methanogenesis.
• the methanogenesis stage produces biogas, a treated effluent and a little sludge whose different uses will be discussed later.
• methanation mainly leads to the production of methane, which can for example be used as fuel for the production of energy.
• the methanization produces a treated effluent which is then subjected to a so-called Stripping and Decarbonation stage.
• the stripping and decarbonation stage results in the production of sludge and a decarbonated effluent.
• the effluent thus stripped and decarbonated is then subjected to all or part of a reverse osmosis filtration step.
• This recycled fraction is between 0 and 400% by weight of vinasses and phlegmasses.
• the fraction of the stripped and decarbonated effluent that is not recycled upstream or head of the methanation is subjected to filtration. Filtration is preferably carried out by reverse osmosis on membranes.
• the stripped and decarbonated methanation effluent is subjected to filtration. It is capable of stopping bacteria and particles of dimensions of about 0.2 ⁇ m and greater. This filtration treatment, especially by reverse osmosis, to stop the bacteria, gives as filtrate a water of very good quality, free of salts, that can be recycled in the neil main production process including without risk of infection which can block the biological activity.
• the fraction of the stripped and decarbonated effluent is subjected to specific effluent treatments, including a biological treatment of carbon for the elimination of carbon monoxide. residual carbon pollution (Option 1) and physico-chemical treatment of phosphorus (Option 2).
• Filtrate, or Permeat, obtained by reverse osmosis filtration is a water that can be recycled and in particular be used as water at the steps of must preparation, biological activity and separation.
• the evapo-concentration condensates (evaporation / concentration) described below may also be used at this level or in other production facilities.
• This filtration is suitable for stopping particle size of the order of 0.2 microns (0.2 microns), especially for example bacteria.
• reverse osmosis In addition to the liquid filtrate constituting recycle water, reverse osmosis also produces a Concentrate or Retentate which For example, it may be subjected to a step of evaporation-concentration or evapo-concentration, in particular by steam heating.
• Option 4 Prior to the evapo-concentration (Option 4), all or part of the concentrate obtained from the reverse osmosis can undergo, optionally (Option 3), a stage of biological treatment of the carbon and nitrogen pollution (also called n Iterrification-denitrification) and / or a stage of physicochemical treatment of phosphorus pollution (dephosphatation). All or part of the concentrate having undergone these biological and / or physicochemical treatment steps is then subjected to evapo-concentration.
• Option 3 a stage of biological treatment of the carbon and nitrogen pollution
• dephosphatation a stage of physicochemical treatment of phosphorus pollution
• evapo-concetration produces sludge.
• This sludge can be valorised (for example for the amendment of agricultural soils) or put in landfill.
• the ionic condensates resulting from the evapo-concentration are used in the form of water at the level of the production premises and / or are recycled upstream of the reverse osmosis filtration.
• the liquid condensates from the evapo-concentration can undergo a stripping step and, after this stripping, a portion of the condensates is used in recycled water in the production process, another part that can be recycled upstream of reverse osmosis filtration and / or another part that can still be recycled upstream of the methanation.
• sludge Various steps mentioned previously lead to the production of sludge. These are, for example, methanation sludges, decarbonation sludges and evapo-concentration sludges, etc.
• these sludges may for example be dehydrated. Sludge can also be burned either "at a loss” by incineration or by combustion for energy recovery.
• Sludge can still be valorised (production of components for the amendment of agricultural soils, methanisation of sludge and production of biogas, or other) or landfill.
• the methanation treatment that comprises the acidogenesis step and a methanogenesis step is carried out in an upward flow through a slurry of sludge fixed on a support or a slurry of flocculated or granular sludge constituted by compact aggregates of bacteria and or granules of a mean diameter generally greater than 0.1 mm.
• the phase IICIDE (COPRODU IT 1) is introduced into a reactor for example in the lower part by a network of perforated pipes.
• the liquor phase liquor feed can be advantageously drawn.
• the methanation reactor is closed for anaerobic reaction.
• a biogas outlet is provided at the top.
• Biogas composed mainly of methane is used, for example, for the production of electrical energy, using a turbine or any other suitable device, and / or for producing heat.
• a reactor also referred to igesteur of this type is known as the "Anapulse" and is described in particular in Memento Technique Water Degrémont 1 0 th edition, pages 975-976.
• Such a reactor is usually provided for effluents from breweries, sugary drinks, sweets, starch, paper mill, yeast, etc.
• the anaerobic digestion can also be carried out in reactors with granular sludge fluified, recycled or expanded with single or double stages. Methanation can also be carried out for example in a reactor or "Anaflux" type reactor which is a culture digester fixed on a light support in the reactor.
• a reactor, also called a digester, of this type is described especially in the Degrémont Water Technical Memento, 10 th edition, pages 977-978.
• Such a reactor is usually provided for effluents from breweries, sugary drinks, sweets, starch, paper mill, yeast, etc.
• the anaerobic digestion can also be carried out for example in a reactor or "Anafiz” type digester which is a reactor or culture digester fixed on a packing (for example in plastic, polypropylene, polyethylene), ordered or in bulk.
• a reactor, also called digester, of this type is described in particular in the Degrémont Water Technical Memo 9 th edition, pages 753 to 756.
• the methanation can be carried out industrially, for example in a granular sludge reactor, or in a fluidized bed reactor, which considerably reduces the residence time. anaerobic digestion. This duration becomes less than about six days and for example of the order of three to four days, while generally it is greater than twenty days, and could reach thirty days and more, for the treatment by methanization of the liquid phase or vinasse as is at the outlet of the distillation column
• the effluent from methanation is subjected to the stripping and decarbonation step in a closed and deodorized tank.
• a stream of gas, usually air, is blown into the bottom of the tank to remove carbon dioxide (CO 2 ) and oxidize the hydrogen sulfide gas (H 2 S) that may be present in the effluent to a deodorization treatment.
• the effluent is then decarbonated.
• the treatment or stripping-decarbonation stage notably makes it possible to recycle an effluent into the methanizer that is low in calcium and magnesium, which would tend to be deposited on granular sludges or biomass supports, on biomass support materials and sludge aggregates, with the result that the efficiency of removal of carbon pollution is reduced as a result of biological and hydraulic problems.
• the invention thus provides a solution to several technical problems encountered during anaerobic digestion according to the prior state of the art: the yields of removal of the COD and BOD 5 obtained in the methanation reactors were insufficient, malfunctions related to inhibition phenomena because of high concentrations and higher or close to the toxicity thresholds of certain components such as MES, anions, cations, did not allow to achieve favorable energy balances of facilities;
• the biogas produced is "clean", in particular with respect to hydrogen sulphide H 2 S.
• the reduction of sulphates in the vinasses makes it possible to avoid the harmful aspects of H 2 S, in particular during methanation (odor, corrosion, and pollution in the form of SO 2 ).
• H 2 S it is a part of the substrate that is normally used for the production of methane, which is "used” for the conversion of SO 4 2 " to H 2 S.
• NGL Global nitrogen (NF EN ISO 11905-1)
• Nitrate (NF EN ISO 13395, NF EN ISO 10304-1)
• Table 1 describes, by way of example, the composition of the liquid phase (COPRODUIT 1) after separation upstream of the extraction and resulting from the production of bioethanol from starchy, sacchariferous or lignocellulosic plants.
• COPRODUIT 1 the composition of the liquid phase (COPRODUIT 1) after separation upstream of the extraction and resulting from the production of bioethanol from starchy, sacchariferous or lignocellulosic plants.
• Table 2 presents the operating conditions for the implementation of the treatment steps by acidogenesis and by methanogenesis.
• the effluent is stripped in order to eliminate CO 2 and increase the pH and thus reduce the quantities of reagent to be introduced for decarbonation.
• lime is added (0.1 to 5 g / l) so as to increase the pH to 10-11.
• the mixture is stirred for 0.5 to 5 hours. After reaction, a settling stage makes it possible to separate the flocs formed which will decant at the bottom of the tank and the decarbonated effluent is recovered at the surface.
• a fraction of the stripped and decarbonated effluent (0 to 400% by mass of the vinasses and the phlegmasses) is recycled at the head of anaerobic digestion in order to reduce the TH in the reactor, to limit the increases of pH and to get rid of the precipitation phenomena that may be unfavorable for the anaerobic biological process.
• this stripping-decarbonation step also protects the reverse osmosis filtration stage of the mineral precipitation phenomena of carbonate.
• the fraction of the stripped and decarbonated effluent that is not recycled to the methanizer is directed to reverse osmosis treatment in order to reduce or eliminate almost completely the following parameters:
• the treatment scheme (sum of all treatments) as defined, namely the pretreatment of the fermented must before extraction, the anaerobic digestion treatment, the stripping-decarbonation treatment, and the recycling of a fraction of the stripped effluent and decarbonated at the head of anaerobic digestion makes it possible to increase the inhibitory limit values for the biological processes in the raw materials, compared with the values usually defined for anaerobic digestion treatment.
• This threshold threshold increase is possible because of the high performance of the elimination treatments implemented.
• the characteristics of the vinasses after distillation of the fermented musts are strongly influenced by the composition of the fermented musts and, in particular, by the concentration of MES; in fact, the MESs of musts, consisting mainly of organic materials, will, during the distillation, be heated to high temperature and for a significant part modified and solubilized (for example, Maillard reactions leading to the formation of non-biodegradable or even toxic compounds ); other compounds such as, for example, proteins, amino acids, nitrogen and the organic phosphorus participating in the colloidal and soluble fraction of fermented musts before distillation will also suffer the effects of temperature (for example, Maillard reactions) resulting in the formation of non-biodegradable or even toxic compounds.
• temperature for example, Maillard reactions
• the theoretical 100% rate corresponds to all the dry matter initially contained in the musts. For example, it is about 55 to 65 kg per hectolitre of alcohol produced.

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