EP4311993A1 - Procédé de séchage de produits en bois permettant de produire des produits en bois à émission réduite de cov - Google Patents

Procédé de séchage de produits en bois permettant de produire des produits en bois à émission réduite de cov Download PDF

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Publication number
EP4311993A1
EP4311993A1 EP22186666.8A EP22186666A EP4311993A1 EP 4311993 A1 EP4311993 A1 EP 4311993A1 EP 22186666 A EP22186666 A EP 22186666A EP 4311993 A1 EP4311993 A1 EP 4311993A1
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EP
European Patent Office
Prior art keywords
wood
amount
wood product
steam
drying
Prior art date
Legal status (The legal status 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 status listed.)
Pending
Application number
EP22186666.8A
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German (de)
English (en)
Inventor
Bernd Bungert
Thomas HEINE
Martin SCHWENDY
Christian DÜMICHEN
André HENNIG
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Fiberboard GmbH
Original Assignee
Fiberboard GmbH
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 Fiberboard GmbH filed Critical Fiberboard GmbH
Priority to EP22186666.8A priority Critical patent/EP4311993A1/fr
Priority to US18/848,747 priority patent/US20250216153A1/en
Priority to KR1020247032970A priority patent/KR20240159932A/ko
Priority to MX2024010325A priority patent/MX2024010325A/es
Priority to CN202380025661.7A priority patent/CN118974499A/zh
Priority to PCT/EP2023/068350 priority patent/WO2024022754A1/fr
Priority to EP23739181.8A priority patent/EP4551882A1/fr
Priority to CA3251960A priority patent/CA3251960A1/fr
Publication of EP4311993A1 publication Critical patent/EP4311993A1/fr
Pending legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/005—Treatment of dryer exhaust gases
    • F26B25/006—Separating volatiles, e.g. recovering solvents from dryer exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B21/00—Arrangements for supplying or controlling air or other gases for drying solid materials or objects
    • F26B21/30—Controlling, e.g. regulating, parameters of gas supply
    • F26B21/33—Humidity
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B21/00—Arrangements for supplying or controlling air or other gases for drying solid materials or objects
    • F26B21/30—Controlling, e.g. regulating, parameters of gas supply
    • F26B21/37—Velocity of flow; Quantity of flow
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/22—Controlling the drying process in dependence on liquid content of solid materials or objects
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B2200/00—Drying processes and machines for solid materials characterised by the specific requirements of the drying goods
    • F26B2200/24—Wood particles, e.g. shavings, cuttings, saw dust

Definitions

  • the invention relates to a method for drying wood products to produce wood products with reduced VOC emissions.
  • the present invention relates in particular to a method for producing wood products, the method allowing improved removal of VOCs from the wood product, in particular from the wood, through an improved drying step.
  • Emission problems are known for boards in the wood-based materials industry, such as chipboard, OSB boards, or pallets, but also in the production of pellets from wood chips or sawn wood. These occur, for example, after drying in the exhaust air and/or in the finished product itself.
  • chipboard and OSB boards for example, the so-called "blue haze” is known as a phenomenon of the exhaust gas. These are aerosols from dust with condensing VOCs, especially terpenes. It is also generally known that chipboard and OSB boards emit VOCs in the interior.
  • Primary emissions can include, for example, ingredients in the wood, such as terpenes, for example alpha-pinene, delta-3-carene, but also formaldehyde, for example from the glue contained or organic acids, if finished panels are intended.
  • secondary emissions also arise, i.e. emissions from reaction products of the substances contained in the product, for example through reactions in the finished, possibly already used product or through reactions in the indoor air of primary emissions with other airborne compounds, such as the reactive species ozone , hydroxyl radicals, nitrogen oxides or sulfur dioxide.
  • An example is oxidation reactions of terpenes with ozone. At the Reaction of the monoterpene limonene with ozone can produce, for example, formic acid and acetic acid.
  • wood contains fats or fatty acids. These are gradually reduced to aldehydes.
  • the key substances here are hexanoic acid and hexanal.
  • Secondary emissions can therefore consist of secondary ingredients, such as aldehydes from the breakdown of fats or fatty acids contained in wood, for example hexanoic acid from triglycerides, which can react to form hexanal.
  • Related substances include formaldehyde from formic acid, acetaldehyde from acetic acid, etc.
  • Such a method makes it possible in a particularly advantageous manner to efficiently reduce environmentally harmful and/or health-damaging VOC emissions in the production and/or use of wood products. This allows low-emission further processing and usability of the wood products as well as problem-free use of the VOCs removed from the wood.
  • VOC Volatile Organic Compounds
  • VOCs described in this process are terpenes, which occur as wood oil in the wood. Examples include the following substances, which can occur in the weight percentages given in brackets based on the VOCs contained: ⁇ -pinene (20-70%), ⁇ -pinene (5-20%), limonene (1-5%) , camphene (1-5%), phenol (0.2-2%).
  • VOCs can be understood to mean organic acids, present as free acids or bound as fats, i.e. typically as triglycerides, such as formic acid, acetic acid, hexanoic acid, etc.
  • VOCs also include the corresponding subgroups, in particular VVOC (very volatile organic compounds, highly volatile organic compounds), SVOC (semi volatile organic compounds, poorly volatile organic compounds) and MVOC (microbial volatile organic compounds, biolog. volatile organic compounds).
  • wood products also referred to as wood products, and in particular to dry wood-containing products.
  • a product can be understood to mean an end product as well as an intermediate product that still requires further processing into a final product.
  • wood-containing product or wood product means that the product contains at least some wood or only consists of wood. Examples include WPC products (Wood Plastic Composite).
  • the method described here includes providing a wood product.
  • the wood products within the meaning of the invention can be intermediate products or end products. Examples include OSB boards, chipboard, pallets, flexboard products, i.e. insulation mats and rolls, or even pellets or sawn wood.
  • Fiberboards produced using the dry process for example with a bulk density of less than 650 kg/m 3 , which can be referred to as light MDF (LDF) or with a bulk density of less than 550 kg/m 3 as ultra-light MDF (ULDF), can also be used.
  • LDF light MDF
  • ULDF ultra-light MDF
  • the wood products can include products produced using the dry process.
  • a dry process can be understood as one in which no water is added during production.
  • a dry process in the sense of the present invention is therefore to be understood in particular as a process in which the wood product, after being made available, is in the form of lumpy parts or particles that are smaller than the wood trunk or sections of the wood trunk, for example wood chips, shavings, strands or sawn wood are not further treated with liquid or vaporous water, as is typically the case in the production of MDF/HDF when cooking at elevated temperatures before the refiner.
  • glue or paraffin emulsion in aqueous suspensions or emulsions is excluded from this treatment.
  • a dry process does not involve suspending wood chips in liquid water or heating lumpy parts with water or steam.
  • the wood used is not fundamentally limited, for example, wood selected from pine wood, spruce wood, lark wood, birch wood, beech wood, dead oak wood, alder wood, etc. can be used, but is not limited to this.
  • method step b) includes drying the wood product by thermally treating it, i.e. under the influence of temperatures that are higher than room temperature.
  • the wood product can generally be treated in a dryer.
  • the drying or process step b) is designed in two stages and includes process steps b1) and b2).
  • process steps b1) and b2) can be carried out in two successive, for example immediately successive, drying devices or separate drying areas.
  • known drum dryers for example with built-in coiled pipes, can be used as drying devices.
  • partial steam distillation can take place as step b1) in a knife ring chipper, with pneumatic conveyance to the dryer, in a screw apparatus, in a belt dryer, in a preferably small drum dryer or similar.
  • a first drying step optionally involves adding water vapor to the wood product and drying the wood product while removing a first amount of water vapor.
  • the first amount of water vapor can be applied with largely exclusion of air by evaporating the partial amount of water vapor based on the water contained in the wood product.
  • the water used for process step b1) can come entirely from the wood to be dried, which, as described in more detail below, can be determined depending on at least one specification of the wood product provided in process step a). It can therefore be advantageous that no steam is added in process step b1) or that the wood is not moistened before or during process step b1).
  • steam distillation or partial steam distillation can take place by removing a defined amount of steam.
  • VOCs such as terpenes
  • water vapor is optionally added in a predetermined first quantity range and removed in a predetermined second quantity range in such a way that a lower limit and an upper limit of at least one of the first quantity range and the second quantity range are determined depending on at least one specification of the in Process step a) provided wood product is selected.
  • the invention is therefore based, as described above, in particular on the fact that by separating steam from the process according to process step b1), VOCs can be efficiently separated from the production stream, since they accumulate in the steam in step b1). Appropriate vapor separation therefore reduces the emission of VOCs, for example as exhaust gases or as vapors from the manufactured product.
  • the entire wood is usually brought to boiling temperature to dry in order to remove the water from the wood.
  • Exemplary boiling conditions include approximately 1 bar at 100 °C. According to the state of the art, this is done up to a predeterminable target moisture content without considering the VOCs contained. If an exemplary water content of the wood is assumed to be 50% by weight and heating from 20 ° C to 100 ° C, an amount of heat of around 1,406,000 kJ must be applied, for example using a contact dryer or a convection dryer. The like that However, the VOCs expelled are very diluted, so that they can hardly be economically isolated or reused in any other way.
  • step b1) in a first step only the VOCs are removed without significantly drying the wood, which in turn can be done by heating the wood to 100 ° C with evaporation of small amounts of water, approximately 1% of the total amount of water in the wood, is sufficient an exemplary amount of heat under comparable conditions of 22,000 kJ to remove essentially all VOCs.
  • step b1) can be completed after the VOCs have been removed without taking the residual moisture of the wood into account. This shows that VOCs can be removed from the wood with a very low-energy dryer that also requires very little installation space, and that a highly concentrated amount of steam is also produced with regard to the VOCs.
  • Heating the wood to remove the VOCs according to process step b1) can be done in various ways, such as supplying heat through contact, preferably with extensive exclusion of air. Wood oil can then be obtained particularly preferably using the steam. The latter is also possible with heating by adding steam. Superheated steam, for example at temperatures of, for example, 140 ° C, can be used, although avoiding condensation may be preferred. Heating is also possible by supplying warm air, for example at temperatures of 160°C. Condensation can in turn produce wood oil.
  • step b1 The same applies to the amount of water vapor supplied, as this should be sufficiently large to effectively remove the VOCs, but should be as small as possible in order to reduce the size of the dryer and the energy requirement for step b1) or at Condensation of at least part of the water vapor supplied in step b1) also keeps the energy expenditure in step b2) as low as possible.
  • the process described here also takes advantage of the fact that terpenes, the most important VOC in this process, have a boiling point of over 150 ° C, but it was still found that even exhaust steam streams or, in general, steam streams with temperatures below 100 ° C contain a significant amount of volatiles may contain organic substances and especially terpenes. This is due to the formation of the heteroazeotropes as described above. It is therefore advantageous in the method described here that the total amount of steam separated is taken into account, regardless of its origin or the local separation point.
  • the separation of steam streams can in principle be carried out using methods from the prior art and it is advantageous that the steam is treated to collect the VOCs and is not released into the environment along with the VOCs.
  • the steam can be separated using excess pressure or negative pressure.
  • water vapor is optionally added in a predetermined first quantity range and removed in a predetermined second quantity range such that a lower limit and an upper limit of at least one of the first quantity range and the second quantity range depend on at least one specification of the wood product provided in method step a). is chosen, can be implemented in a variety of ways, as described in greater detail below.
  • a further drying step takes place according to process step b2), namely the drying of the wood product with the removal of a second amount of water vapor up to a predeterminable target moisture content.
  • the target moisture is the moisture content that can or should be adjusted for the wood product through drying.
  • This second drying step can be carried out as is generally known for such wood products in order to bring the wood products to the desired residual moisture.
  • this step can also be carried out using heat or using a conventional technical drying apparatus.
  • Process step b1) can be tailored to the removal of VOCs, which can combine low energy input with efficient VOC removal.
  • step b2) drying can then be carried out in the usual manner in order to achieve the desired final moisture.
  • step b1 By designing the drying as a two-stage process, a particularly simple implementation into existing processes can also be made possible, since the partial steam distillation according to step b1) can be easily inserted before the usual step b2). This can be done, for example, by inserting an additional dryer in front of the actual dryer in conventional processes.
  • the additionally introduced dryer can have very small dimensions, for example in a range of less than or equal to 5% by volume of drying volume compared to a conventional dryer.
  • the residence time of the wood in the dryer required for step b1) is extremely short, so that a large amount of VOCs can be removed very quickly. In addition, even a very small amount of energy is enough to remove the VOCs.
  • step b1) which is spatially separate from method b2)
  • the VOCs can also be collected particularly easily, with the amount of steam collected being very small, in particular in comparison to the possibility of collecting the total amount of steam produced during the entire drying process.
  • An efficient collection of VOCs from the steam stream of a conventional dryer is actually not possible.
  • the concentration of VOCs in the amount of steam separated at b1) is also comparatively high, so that isolation is simplified.
  • steps b1) and b2) are carried out one after the other in a dryer.
  • the process can be carried out in a particularly low-energy and therefore resource-saving manner, since only a small input of energy is necessary to evaporate the VOCs and remove them from the wood due to the formation of a heteroazeotrope as described above.
  • internal heat recovery can of course take place, for example by cooling exhaust air or exhaust steam.
  • a continuous separation of the steam includes, for example, an uninterrupted separation or a continuous periodic separation, i.e. comprehensively definable periodically recurring pauses.
  • the present method also offers advantages over methods known from the prior art. For example, it is known to carry out a process known as UTWS drying or eco dry, in which unwanted substances are removed using high energy. However, the entire drying process takes place with superheated steam. Air introduced makes condensation more difficult. Retrofitting existing systems is rarely technically possible and does not make practical commercial sense. In contrast, however, the process according to the invention allows significantly shorter residence times in the dryer for step b1), smaller amounts of gas separated off in the VOC separation and improved condensation conditions. Drying with superheated steam is known from the production of pellets. However, similar to the UWTS process, the entire drying is carried out with superheated steam, which also results in the advantages described above compared to this process according to the invention.
  • UTWS drying or eco dry in which unwanted substances are removed using high energy.
  • the entire drying process takes place with superheated steam. Air introduced makes condensation more difficult. Retrofitting existing systems is rarely technically possible and does not make practical commercial sense.
  • the process according to the invention allows significantly shorter residence times in the dryer
  • one specification or a plurality of specifications may be selected from the following specifications.
  • the amount of both wood and steam can be the absolute amount in a batch process, or the amount of both wood and steam can be the amount per unit of time in a continuous process.
  • the amount of wood has a significant influence on the VOCs introduced into the process by the wood and thus equally on the VOCs to be discharged, so that the amount of wood in the wood product should be taken into account when determining the amount of steam to be separated.
  • the amount of wood can be equally important for the amount of water vapor introduced as well as for the amount of water vapor discharged. In this way it can be ensured that, on the one hand, the VOCs are removed as completely as possible, but on the other hand, in process step b2), excessively unused water vapor introduced in b1) does not have to be removed again.
  • VOCs for example terpenes and/or fatty acids or fats
  • the amount of VOCs present in the wood product may be considered as a weight percent relative to the amount of wood product.
  • VOCs present in a certain amount of wood can depend on the specific type of wood used.
  • the amount of steam to be introduced and/or separated can be reduced particularly reliably, since it is ensured that fluctuations in the components that occur during the separation of the steam do not result in too little steam being separated off and thus an undesirably high content of VOCs exit.
  • the amount of steam to be separated and produced can still be safely reduced reliably and without the danger described above.
  • the amount of VOCs contained in the wood product may further be preferred that the amount of VOCs contained in the wood product provided in method step a) is determined by examining the wood product used or based on the type of wood product used, in particular the wood contained , is estimated.
  • Determining the amount of VOCs by examining the wood product can enable a particularly precise determination of the VOCs contained in the wood product, so that the determination of the amount of steam to be introduced and/or separated can also be carried out very precisely.
  • the respective amount can be determined in a manner known per se by analyzing the components of the wood product. This can be advantageous, for example, because the VOC content can be reduced simply due to evaporation during storage or fluctuations in the VOCs contained in the same type of wood can occur.
  • An assessment of the components of VOCs contained in the wood product based on the type of wood product used, i.e. in particular taking into account what type of wood the wood product has, can allow a particularly simple determination of the components, whereby the effort can be kept very low.
  • This embodiment can be based in particular on the fact that different types of wood, for example birch or spruce, often have a different amount of VOCs, but the amount contained depends on the type of wood is characteristic. This means that the amount of VOCs can be estimated in advance by knowing the wood used, without having to carry out any analysis.
  • the amount of steam added and/or separated can be determined with a definable safety factor, i.e. a definably larger amount of steam can be added and/or separated than according to the data used Quantity ranges necessary. This also allows a particularly safe and reliable reduction in the amount of VOCs and/or fatty acids discharged from the process.
  • the total amount of steam separated off in process step b1) is in a quantity range of 0.5 to 100 times the mass, preferably 0.5 to 50 times the mass, particularly preferably 0.5 to 10 times the mass. times the mass, based on the VOC amount of the wood product provided.
  • the amount of steam to be supplied can be in a similar range to the amount of steam removed. However, this depends on the process control and the type of heat supply. It is conceivable to heat the wood product with extensive or (almost) complete exclusion of air and only convert the water contained in the wood into the vaporous state. Alternatively, heating can be carried out using saturated or superheated steam. If the latter is the case, then the amount of steam to be supplied is correspondingly higher. It follows that the quantity range of water vapor to be supplied is in a quantity range of 0-300 times the mass, preferably 0-150 times the mass, particularly preferably 0-30 times the mass, based on the VOC quantity of the wood product provided.
  • This amount is significantly below the amount of steam that would be separated if the wood product were dried to the final moisture in a single drying step, but is surprisingly sufficient to remove essentially the entire amount of VOCs or fatty acids from the wood product and thus reduce the VOC To significantly reduce emissions in the process described here. It has therefore been shown that, for example, if the process described here or the amount of steam separated in the process is adjusted accordingly, a surprisingly small amount Amount of steam can be separated that is sufficient to solve the problem according to the invention.
  • the total amount of steam separated off in process step b1) is in a quantity range of 0.001 to 0.2 times the mass, preferably 0.001 to 0.1 times the mass, particularly preferably 0.001 to 0, 02 times the mass, based on the dry mass of the wood product provided.
  • the amount of steam introduced is in a range of 0-0.6 times the mass, preferably 0-0.3 times the mass, particularly preferably 0-0.1 times the mass, based on the dry mass of the wood product provided.
  • This embodiment is based on the fact that the dry mass of the wood product can also be a good indicator for determining the amount of steam that may need to be introduced and/or separated. Even with such a correlation, the amount of steam to be separated is significantly below the amount used in solutions from the prior art through a one-step drying, but is also surprisingly sufficient to remove almost the entire amount of VOCs from the process and thus significantly reducing VOC emissions in the process described here for producing wood products.
  • the dry matter of the wood product or wood refers in particular to absolutely dry wood (atro), as is common in wood processing.
  • the dry matter of wood used can in turn be determined analytically or estimated based on known data for the type of wood used.
  • the mass can be easily determined in continuous or batch processes, as an amount per unit of time or as an absolute amount, as described above.
  • such small amounts in process step b1) enable residence times in a dryer of a few seconds, for example less than 10 seconds. This is made possible because, for example, drying by only a few% is sufficient, for example 3%. This also makes it possible to use appropriate dryers with a low volume. This shows the problem-free implementation in existing processes with small sizes and therefore correspondingly low investment costs.
  • process step b1) takes place at least partially with the exclusion of air.
  • the amount of water in the wood can be sufficient as a carrier substance for the VOCs.
  • water vapor removed in process step b1) is continuously separated from the process at at least one steam emission point. This allows a particularly efficient process and can be carried out under stationary conditions without much control effort.
  • the VOC-containing water vapor removed according to process step b1) is collected and, if necessary, one or more components are further treated.
  • the process can not only serve to reduce VOC emissions, but the process can be carried out much more economically due to the possibility of collecting separated vapor streams and, if necessary, treating them further. This is because the materials contained in the steam stream or other properties of the steam stream, such as its heat, can be used in the process or other processes so that costs and resources can be saved.
  • hydrosol is isolated for further treatment.
  • hydrosol is generally understood to mean the aqueous phase obtained after condensation of the vapor and separation of water-insoluble substances, which may contain corresponding water-soluble components, such as formaldehyde or short-chain organic acids or similar.
  • the separated vapor or one or more components may also be advantageous for the separated vapor or one or more components to be further treated by combustion or exposure to high temperatures, adsorption, absorption, membrane technology methods, condensation, crystallization or other suitable process engineering methods.
  • Burning or exposing to high temperatures enables, for example, thermal afterburning and thereby energetic use of the VOCs contained in the separated steam stream.
  • the other methods mentioned can all relate to the isolation or separation of individual substances.
  • At least one of the heat of a material stream occurring in the process and the heat of a separated steam stream can be further used energetically in the process.
  • the energy inherent in the material flow can be further used in the form of heat, in particular to heat other material flows or to carry out drying. This step can also improve economic aspects of the method according to the invention and thus save costs and resources.
  • a wooden product is provided.
  • the wood product is formed in particular by a drying process and should then be dried.
  • Two dryers 12, 14 are provided for this purpose. The drying therefore takes place in two stages, with the dryer optionally adding 12 steam to the wood product in one first quantity range is added, which should be shown by the arrow 16 and the wood product is dried while removing a second quantity range of water vapor.
  • the latter should be represented by arrow 18.
  • heteroazeotropes form from the VOCs in the wood product and the water, which are carried out with the water vapor.
  • water vapor is optionally added in a predetermined first quantity range and removed in a predetermined second quantity range such that a lower limit and an upper limit of at least one of the first quantity range and the second quantity range is selected depending on at least one specification of the wood product provided.
  • the partially dried fetch product which has been depleted in terms of VOCs, is passed to the second dryer 14, as indicated by the arrow 20.
  • the wood product is dried by the second dryer 14 with the removal of a second amount of water vapor up to a predeterminable target moisture content, which should be indicated by the arrow 22.
  • the wood product brought to its final moisture content is provided, as shown by the arrow 24.
  • the wood product After providing the wood product with final moisture, the wood product can be finished or further processed.
  • water vapor containing VOC removed can be collected and, if necessary, one or more components can be further treated.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)
EP22186666.8A 2022-07-25 2022-07-25 Procédé de séchage de produits en bois permettant de produire des produits en bois à émission réduite de cov Pending EP4311993A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
EP22186666.8A EP4311993A1 (fr) 2022-07-25 2022-07-25 Procédé de séchage de produits en bois permettant de produire des produits en bois à émission réduite de cov
US18/848,747 US20250216153A1 (en) 2022-07-25 2023-07-04 Method for drying wood products in order to produce wood products with reduced voc emissions
KR1020247032970A KR20240159932A (ko) 2022-07-25 2023-07-04 감소된 voc 방출물들을 갖는 우드 제품들을 제조하기 위해 우드 제품들을 건조하기 위한 방법
MX2024010325A MX2024010325A (es) 2022-07-25 2023-07-04 Procedimiento para el secado de productos de madera para producir productos de madera con emisiones reducidas de cov.
CN202380025661.7A CN118974499A (zh) 2022-07-25 2023-07-04 用于干燥木制品以生产voc排放减少的木制品的方法
PCT/EP2023/068350 WO2024022754A1 (fr) 2022-07-25 2023-07-04 Procédé de séchage de produits en bois pour la production de produits en bois à émissions de cov réduites
EP23739181.8A EP4551882A1 (fr) 2022-07-25 2023-07-04 Procédé de séchage de produits en bois pour la production de produits en bois à émissions de cov réduites
CA3251960A CA3251960A1 (fr) 2022-07-25 2023-07-04 Méthode de séchage de produits de bois afin de produire des produits de bois à émissions réduites de composés organiques volatils

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EP22186666.8A EP4311993A1 (fr) 2022-07-25 2022-07-25 Procédé de séchage de produits en bois permettant de produire des produits en bois à émission réduite de cov

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EP4311993A1 true EP4311993A1 (fr) 2024-01-31

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB242494A (en) * 1925-02-18 1925-11-12 August Baumann Improvements in apparatus for drying wood, lacquered, painted or spatulated articlesand the like
US4026037A (en) * 1975-02-18 1977-05-31 Adolf Buchholz Apparatus for steam drying
EP0743498A2 (fr) * 1995-05-16 1996-11-20 Andritz-Patentverwaltungs-Gesellschaft m.b.H. Procédé de séchage de substances humides, notamment de fibres de bois
WO2004016718A1 (fr) * 2002-08-12 2004-02-26 Jgc Corporation Procede de modification d'une biomasse, biomasse modifiee, boue de biomasse aqueuse et son procede de production, gaz de biomasse modifie et procede de gazeification de biomasse
WO2014165995A1 (fr) * 2013-04-09 2014-10-16 Diacarbon Technologies Inc. Procédé de torréfaction

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB242494A (en) * 1925-02-18 1925-11-12 August Baumann Improvements in apparatus for drying wood, lacquered, painted or spatulated articlesand the like
US4026037A (en) * 1975-02-18 1977-05-31 Adolf Buchholz Apparatus for steam drying
EP0743498A2 (fr) * 1995-05-16 1996-11-20 Andritz-Patentverwaltungs-Gesellschaft m.b.H. Procédé de séchage de substances humides, notamment de fibres de bois
WO2004016718A1 (fr) * 2002-08-12 2004-02-26 Jgc Corporation Procede de modification d'une biomasse, biomasse modifiee, boue de biomasse aqueuse et son procede de production, gaz de biomasse modifie et procede de gazeification de biomasse
WO2014165995A1 (fr) * 2013-04-09 2014-10-16 Diacarbon Technologies Inc. Procédé de torréfaction

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