• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention relates to a hydrothermal liquefaction biomass treatment device comprising: - a mixing unit (1) of the biomass and water to form a fluid; an injection pump (2) for the fluid downstream of the mixing unit (1); a hydrothermal liquefaction reactor (3) for the fluid, downstream of the injection pump (2); - a separation unit (4), downstream of the hydrothermal liquefaction reactor (3), the separation unit (4) comprising an aqueous phase outlet and an organic phase outlet; an electrolyser (9), downstream of the aqueous phase outlet of the separation unit (4). The present invention also relates to the method of transforming biomass using this device.
    公开号:FR3035404A1
    申请号:FR1553601
    申请日:2015-04-22
    公开日:2016-10-28
    发明作者:Maxime Deniel；Geert Haarlemmer
    申请人:Commissariat a lEnergie Atomique CEA；Commissariat a lEnergie Atomique et aux Energies Alternatives CEA；
    IPC主号:
    专利说明:

    [0001] FIELD OF THE INVENTION The present invention relates to a device and a method for transforming biomass. This transformation is carried out 1, x7 hydrothermal liquefaction and by electrolysis. It makes it possible to generate, from the biomass, the hydrocarbon biofuel. ANTERIOR STATE OF. TECHNIQUE The generation of biofuel has been the subject of much work including the transformation of organic matter, such as biomass, into alkanes. Conventional processes may involve treating the biomass by hydrothermal liquefaction to obtain a mixture containing: - oil; - the tank; an aqueous phase containing el-unique and inorganic products; and gases. Subsequent steps make it possible to separate these different compounds resulting from the transformation of the biomass by hydrothermal liquefaction. The oil obtained corresponds to a mixture consisting essentially of hydrocarbons (carbon and hydrogen compounds) and oxygenated organic compounds of ketone, phenolic, fatty acid ester or fatty acid type. The chariot corresponds to a solid organic residue. It comprises insoluble organic polymers and inorganic compounds initially present in the biomass. The hydrothermal liquefaction process is carried out in water, under pressure and at a temperature of the order of 280 to 350 ° C. The presence of hydrogen promotes its implementation. It can be carried out in acidic, neutral or more generally basic medium. After the hydrothermal liquefaction, the aqueous phase can be partially recycled to initiate a new hydrothermal liquethetion cycle. The aqueous phase is rich in organic molecules having affinities with water because of their high oxygen content and polarity. These include carboxylic acids, phenolics, alcohols and ketones. However, organic and inorganic species accumulate in the aqueous phase. It is usually necessary to remove some of the aqueous phase to remove these water soluble compounds that can not be converted by hydrothermal liquefaction. This constraint represents one of the main disadvantages associated with hydrothermal liquefaction. It corresponds to the increase, during the recycling of the aqueous phase, of the level of inorganics in the biomass / recycled water mixture. The oil produced by the hydrothermal liquefaction process is viscous and generally contains 10 to 20% by weight of oxygen in the form of oxygenates. On the contrary, fossil oils hardly include oxygen. They consist essentially of hydrocarbons. The presence of oxygen compounds can be problematic because they reduce the calorific value and can contribute to the aging of the oil. Their removal is generally carried out by conventional hydrotreating techniques in the presence of a catalyst and hydrogen under high pressure. However, this type of purification requires specific equipment. Moreover, the presence of these oxygenated compounds decreases the overall yield of biofuel generation, as well as the organic compounds present in the aqueous phase.
    [0002] The present invention makes it possible to solve the problems related to the presence of organic compounds in the aqueous phase, while improving the oil production efficiency from the transformation of the biomass. For that. the Applicant has developed a device and a process combining hydrothermal liquefaction of biomass and the electrolysis of the aqueous phase resulting from hydrothermal liquefaction.
    [0003] SUMMARY OF THE INVENTION The Applicant has developed a device and a method for improving the transformation of biomass by hydrothermal liquefaction and by electrolysis.
    [0004] The combination of hydrothermal liquefaction and electrolysis makes it possible to improve the treatment of aqueous effluents by using them to increase the overall yield of the biomass treatment process.
    [0005] Biomass refers to matter of animal, plant, fungal or microorganism origin. More specifically, the present invention relates to a hydrothermal liquefaction biomass treatment device, comprising: a unit for mixing biomass and water to form a fluid; a fluid injection pump downstream of the mixing unit; a hydrothermal fluid liquefaction reactor, downstream of the injection pump; a separation unit, downstream of the separation reactor, comprising an aqueous phase outlet and an organic phase outlet; an electrolyser, downstream of the aqueous phase outlet of the separation unit. The hydrothermal liquefaction reactor is capable of transferring the biomass into a mixture of oil, tank, gas, and aqueous phase comprising oxygenated organic compounds. As already indicated, the oil corresponds to a mixture consisting essentially of hydrocarbons (carbon and hydrogen compounds) and oxygenated organic compounds such as ketones, phenolics, fatty acid esters or fatty acids. i.e char corresponds to. a solid organic residue. It comprises insoluble organic polymers and inorganic compounds initially present in the biomass. The electrolyser can deoxygenate the organic molecules present in the aqueous phase to form hydrocarbon compounds (hydrocarbons), advantageously alkanes.
    [0006] Advantageously, the device according to the invention comprises, downstream of the electrolyzer, a connection to the mixing unit or between the mixing unit and the injection pump. According to another embodiment, the device comprises, downstream of the electrolyser, a connection to the hydrothermal liquefaction reactor. In this case, the aqueous phase from the electrolyzer is advantageously pressurized before introduction into the hydrothermal liquefaction reactor. She then undergoes a preswaging stage.
    [0007] This connection downstream of the electrolyser makes it possible to recycle the electrolyzed aqueous phase in a new cycle of biomass transformation. The device according to the invention may also comprise a separation unit downstream of the electrolyser. It makes it possible to separate the aqueous phase from the organic molecules generated in the electrolyser. This separation unit is advantageously a settling unit. It is advantageously located upstream of the connection allowing the recycling of the aqueous phase in the hydrothermal liquefaction process.
    [0008] The present invention also relates to a method of transforming biomass. This method implements the device according to the invention. It comprises the following steps: preparation of a fluid by mixing biomass with water; Injecting this fluid into a hydrothermal liquefaction reactor; transformation of biomass in the hydrothermal liquefaction reactor; obtaining a fluid comprising oil, the tank, gases, and an aqueous phase containing oxygenated compounds; separation of the oil, cis, gas, and aqueous phase containing oxygenates; formation of hydrocarbons by electrolysis of the aqueous phase containing oxygenated compounds. The term "oxygenated compound" refers to an organic compound comprising carbon, hydrogen and oxygen atoms.
    [0009] In general, the oxygenated compounds of the aqueous phase derived from the hydrothermal liquefaction reactor are, alone or as mixtures of ketones, phenolic compounds, and carboxylic acids. These compounds may also include traces of alcohols.
    [0010] The hydrothermal liquefaction reactor generally comprises a heat exchanger, a heating unit and an autoclave in which the transformation of the biomass is carried out.
    [0011] The heat exchanger preheats the fluid before the heating unit and before its introduction into the autoclave. The conversion of the biomass in the hydrothermal liquefaction reactor is advantageously carried out at a temperature between 250 and 350 ° C, more preferably between 300 and 310 ° C. This temperature corresponds to the conditions within the autoclave. In general, the electrolysis of the aqueous phase also generates hydrogen. The hydrogen thus formed can be removed during or after the electrolysis step. It can be used in a post-treatment step of the oil obtained during the separation step. In this case, the hydrogen is advantageously used in a post-treatment of the hydro-deoxygenation type. The hydrocarbons formed by electrolysis can be separated from the aqueous phase, advantageously by decantation. The electrolysed aqueous phase, and optionally separated from the electrolytically generated hydrocarbons, can be recycled into a new biomass transformation cycle. The electrolyzed aqueous phase is then used to prepare the fluid which is injected into the hydrothermal liquefaction reactor. Advantageously, the fluid injected into the hydrothermal liquefaction reactor has a basic pH, advantageously between 8 and 10.
    [0012] In addition,. the fluid preparation step may comprise the addition of a base, for example sodium or potassium hydroxide or carbonate. Other bases are likewise. conceivable.
    [0013] The invention and the advantages thereof will become more apparent from the following figures and examples given in order to illustrate the invention and not in a limiting manner. DESCRIPTION OF THE FIGURE FIG. 1 schematically illustrates a conventional device for hydrothermal liquefaction of biomass. FIG. 2 schematically illustrates a device according to the invention allowing the hydrothermal liquefaction of the biomass and the electrolysis of the aqueous phase resulting from this hydrothermal liquefaction.
    [0014] DESCRIPTION OF THE INVENTION In a conventional hydrothermal liquefaction process, the biomass is generally mixed with water and a NaOH or Na2CO3 base in a mixing unit (1) to form a fluid. This fluid is then injected into a hydrothermal liquefaction reactor via a pump (2) (FIG. 1). This fluid can be prepared under ambient temperature and pressure conditions, for example at 10 Pa between 20 and 50 ° C. The pump (2) makes it possible to inject the fluid into the hydrothermal liquefaction reactor (3), advantageously at a pressure above the saturating pressure of the water, advantageously between 150 and 200 bar. The injection under pressure makes it possible to maintain a liquid phase in the reactor). In general, the hydrothermal liquefaction reactor (3) successively comprises a heat exchanger (6), a heating device (7) and an autoclave (8). Figure 1 illustrates this embodiment. The heat exchanger (6) ensures the preheating of the fluid from the mixer (1) until a temperature of 150 to 250 ° C. is reached. The heat exchanger (6) provides heat transfer between the fluid from the pump (2) (and thus the mixer (1)) and the outgoing fluid. of the autoclave (8). Thus, the incoming fluid is heated by the outgoing fluid which is cooled.
    [0015] The heating device (7) is used to heat the preheated fluid to the operating temperature of the autoclave (8), generally between 250 and 350 ° C. advantageously between 300 and 310 ° C. This is usually electric or combustion heating, the fuel may be partly the tank from the hydrothermal liquefaction process. Thanks to the heat exchanger (6), which thus has a dual function preheating / cooling sseni ent, the temperature of the fluid leaving the autoclave (8) can pass over.
    [0016] 300C at less than 100 ° C, preferably between 50 and 80 ° C. The temperature is chosen to maintain sufficient fluidity at the outlet of the autoclave (8) and after passage through the heat exchanger (6), typically between 50 and 80 ° C. Once treated by hydrothermal liquefaction in the reactor (3), the fluid comprises an aqueous phase, an organic phase and gases. The fluid leaving the reactor (3) is then treated to separate the aqueous phase (Aq) and the organic phase (H + C) in the separator (4). This separation can in particular be carried out by decantation. The recovered water can then be reinjected into the mixing unit (1) and / or purged via the purge (11). The organic phase is generally a mixture of oil (E) and char (C) (solid organic residue). The oil (H) and the tank (C) are also separated in the unit (4), for example by extraction using at least one solvent which is advantageously polar. This solvent may advantageously be chosen from the group comprising dichloromethane. chloroform, acetone, ethanol, isopropanol, and ethyl acetate. Advantageously, the solvent used has a boiling temperature advantageously less than 100 ° C, more preferably less than 90 ° C. The gases (G) contained in the fluid from the reactor (3) can also be separated from the fluid in the unit (4).
    [0017] Thus, the separation unit (4) separates the aqueous phase (Aq), the tank (C), the oil (11) and the gases (G) contained in the fluid from the reactor (3). .
    [0018] The oil from the separator) typically contains 10 to 20% by weight of oxygen, for example in the form of phenolic derivatives, fatty acid and / or fatty acid esters. Therefore, the quality cic oil, once separated from the tank, can be improved in particular by hydro-deoxygenation (HDO) in the unit (5). The oil is then heated, preferably at a temperature between 300 and 400 ° C. in the presence of a catalyst and hydrogen, advantageously in the presence of 50 to 100 bar of hydrogen. The catalyst is generally a noble metal supported on Al 2 O 3 or ZrO 2. Oxygenated organic compounds in the oil are thus degraded and form water and hydrocarbons.
    [0019] The hydro-deoxygenation makes it possible to eliminate at least a portion of the oxygenates possibly present in the oil from the separator (4). In general, a molecule of dihydrogen is necessary to remove an oxygen molecule in a hydrocarbon. At least part of the water contained in the aqueous phase can also be purged (11) before possible reinjection into the mixer (1). This purge eliminates organic or inorganic compounds that can not be converted by hydrothermal liquefaction in the reactor (3). In general, hydrothennial liquefaction can be carried out in basic, neutral or acidic medium. An acidic pH generally favors polymerization reactions and thus the formation of char. On the other hand, a neutral or basic fold favors fragmentation and oil formation. As a result, the oil (H) / char (C) ratio increases with pH. In addition, the biomass / treated water mixture includes a larger amount of biomass as the pH increases. In a basic medium, for example at a pH of between 8 and 10, the fragmentation of the C 6 sugars makes it possible to obtain C 2 -C 5 compounds which can dimerize. Various carboxylic acids can thus be formed, for example acetic acid (C2), propanoic acid (C3), lactic acid (C3), butyric acid (C4) and levulinic acid (C5). and other derivatives. The degradation of sugars and constituents of lgnine produces ketones and phenol derivatives.
    [0020] The device according to the invention (FIG. 2) makes it possible to recover any organic compounds present in the aqueous phase (Aq) issuing from the separator (4). This device comprises an electrolyzer (9) connected to the output of the separator (4). The units (1) to (5) of the device according to the invention are identical to those of the device illustrated in FIG. 1 and described above. Their operation (temperature, pressure, etc.) is also identical. In addition, the reactor (3) of the device of FIG. 2 advantageously comprises the units (6), (7) and (8) of the reactor of FIG.
    [0021] In the device according to the invention, the aqueous phase coming from the separator (4) is treated in the electrolyser (9) (FIG. 2). This hydrothermal liquefaction treatment device for biomass comprises: a unit for mixing (1) biomass and water to form a fluid; A fluid injection pump (2) downstream of the mixing unit (1); a hydrothermal liquefaction reactor (') of the fluid, downstream of the injection pump (2); a separation unit (4), downstream of the hydrothermal liquefaction reactor (3), the separation unit (4) comprising an aqueous phase outlet and an organic phase outlet; an electrolyser (9), downstream of the aqueous phase outlet of the separation unit. Advantageously, this device comprises, downstream of the electrolyser, a connection to the mixing unit (1) or between the mixing unit (1) and the injection pump (2). Figure 2 illustrates these two embodiments. In general, the electrolyser (9) operates by passing a direct or alternating current between two electrodes positioned in the aqueous phase to be electrolyzed. The electrodes are graphite or metal, for example copper, lead or more preferably platinum. The electrolysis temperature is advantageously between 20 and 60 ° C., advantageously of the order of 40 ° C. The applied voltage is advantageously. between 1 and 10V. The electrolyser (9) may comprise a chan 'device. to achieve the desired electrolysis temperature.
    [0022] Since the invention, the hydrothermal liquefaction, is advantageously carried out in a basic medium, the conductivity of the aqueous phase (Aq) resulting from the hydrothermal liquefaction in a basic medium is typically higher than that resulting from liquefaction in a medium. The aqueous phase (Aq) resulting from the liquefaction in a basic medium is therefore more favorable to be converted in the electrolysis step Electrolysis makes it possible to reduce the amount of oxygen in the compounds. The elimination of oxygen renders these compounds less soluble in water and facilitates their separation from the aqueous phase, in particular by decantation, and the electrolysis of the aqueous phase (Aq) makes it possible to remove the organic phase from the aqueous phase (Aq). in particular to eliminate the carboxylic anions R 1 -C (O-O) -O (IR being a hydrocarbon group) by forming hydrocarbons after dimerization and loss of carbon dioxide according to the following reaction: R 1 -C ( -0) -0 + R2-C (= -O) -O + 2H2O R1-R2 2CO2 ± H2 + 20H More specifically, the reactions taking place at the electrolyser electrodes include: Anode: RI-C 0 -0 + R2-C (-0) -0 R'-02 + 2nd Cathode: 2H20 + 2e H2 ± 20H The electrolysis implemented in the present invention is also known as Kolbe electrolysis. The consumption of the carboxylic acids in the form of anions produces OH anions and increases the pH of the aqueous phase. The reinjection of the electrolyzed aqueous phase downstream of the reactor (3) makes it possible to obtain a fluid having a basic pH in the unit (1). It is thus possible to carry out hydrothermal liquefaction SMS external addition of base. Deoxygenation of ketones by electro-reduction produces alkanes on the cathode.
    [0023] Cathode: R'-C (= O) -R 2 + 4e + 4H + -> R 1 -CH 2 -R 2 + H 2 O 3 3035404 According to an advantageous embodiment, the first cycle of treatment of the biomass is initiated in the presence of a based. Advantageously, the following cycles Ints do not require base addition since reinjection of the electrolyzed aqueous phase makes it possible to obtain a basic pH, advantageously between 5 8 and 10. The base initially introduced during the first cycle is advantageously a base of an alkali metal or alkaline earth metal, especially sodium. The base used is advantageously sodium hydroxide or carbonate.
    [0024] This base of alkali metal (for example sodium) or alkaline earth metal makes it possible to generate salts from the carboxylic acids present in the aqueous phase coming from the separator (4). These carboxylic acid salts are subsequently converted into alkanes by the electrolyser (9) according to the reaction above. Electrolysis also generates hydroxide ions and carbon dioxide which react with each other to form carbonate ions. These carbonate ions can then be reinjected downstream of the reactor (3) to increase the pH of the fluid to be treated by hydrothermal liquefaction. This reinjection can be carried out in the unit (1) or between the unit (1) and the pump (2).
    [0025] The generation of carbonate ions from CO2 and OH hydroxide ions is carried out in the electrolyser (9). The electrolyser not only makes it possible to generate R'-R2 alkanes, but also hydrogen at the cathode, and CO2 and hydrocarbons at the anode (see reactions above). Thus, at least part of the hydrogen consumed in the optional unit (5) may be derived from the electrolysis reaction (9). In this case, the electrolyser (9) can be connected to the unit (5) for treating the oil. As already indicated, the aqueous phase (Aq) from the electrolyser (9) can be injected downstream of the reactor (3). It can also be directly injected into the reactor (3). In this case, the recycled aqueous phase is advantageously preheated and injected under pressure.
    [0026] In the device according to the invention and illustrated by the figure, the unit (5) for treating oil (yarn) issuing from the separator (4) and the unit (10) for decanting the aqueous phase (Aq) electrolyzed are optional. .
    [0027] The unit (5) is used to deoxygenate the oil from the separator (4). The settling unit (10), downstream of the electrolyser (9), makes it possible to separate the hydrocarbon compounds resulting from the electrolysis of the aqueous phase (Aq), before the possible purge (11) and / or the possible reinjection of the aqueous phase upstream of the reactor (3) or into the reactor (3). The biomass treated in the device according to the invention may contain ashes. These can accumulate in the aqueous phase during the recycling steps after passage through the electrolyser. In order to remove these ashes, the aqueous phase can be purged (11) regularly during the cycles. Conventional biomass treatment processes require the addition of compounds such as basic salts to adjust the fold. Their presence generates an aqueous waste stream which requires additional treatment. In addition, some of the biomass remains soluble in these aqueous wastes, which reduces the biomass conversion efficiency. The present invention solves these problems through the presence of electrolyser which processes the aqueous phase. This also makes it possible to at least partially recycle the electrolyzed water and reduce the intake of basic salts. The presence of the electrolyser (9) in the water recycling circuit makes it possible to produce hydrogen, to convert the acids into hydrocarbons and to regenerate the basicity of the fluid injected into the water. reactor (3) hydrothermal liquefaction. EXAMPLE OF CARRYING OUT THE INVENTION A hydrothermal liquefaction reactor is fed with a biomass containing 50% by weight of dry biomass and 50% by weight of water. Typically, the liquefaction reactor has a content of 15-20% solids. Recycle water helps to dilute and create a pumpable mix. The amount of wet material treated is of the order of 2 tons / hour.
    [0028] The calorific value of dry biomass is 5 MW. The yield (in percentage by weight) of the reactor is as follows: 40% of oil (3-4 MW), 30% of tank (2-3 MW), 5% of gas and 20% of material. organic matter contained in the aqueous phase, with a pH of about 8. The amount of char produced (30% by weight) is equal to 300 kg / hour for an energy value of 3 MW.The gas consists mainly of CO2 The aqueous phase is treated in a reactor (200 kg / h) and about 50% by weight of the organic material is in a carboxylic acid form which can be converted to alkanes. Butyric acid (C4H80.2), this represents 0.6 kmol / hour Thus, the electrolyzer can also generate 0.6 kmol / hour of hydrogen according to the following reaction: 2 CH 3 - (CH 2) 2 -C (= 0) -O + 21-T20 -> CH3- (CH2) 2- (CH2) 2 -CH3 + 2CO2 + H2 + 20H The electrical consumption is of the order of 0.7 Mi / mol H2, c ' that is 130 kW.
    [0029] Consequently, the electrolyser makes it possible to generate an additional production of alkanes of the order of 50 kg / hour, or 600 kW.
    权利要求:
    Claims (2)
    [0001]
    REVENDICATIONS1. A hydrothermal liquefaction biomass treatment device comprising: - a mixing unit (1) of biomass and water to form a fluid; an injection pump (2) for the fluid downstream of the mixing unit (1); a hydrothermal liquefaction reactor (3) for the fluid, downstream of the injection pump (2); - a separation unit (4), downstream of the hydrothermal liquefaction reactor (3), the separation unit (4) comprising an aqueous phase outlet and an organic phase outlet; an electrolyzer (9) downstream of the aqueous phase outlet of the separation unit (4).
    [0002]
    2. Device for treating biomass by hydrothermal liquefaction according to claim 1, characterized in that it comprises downstream of the electrolyzer (9) a connection to the mixing unit (1) or between the mixing unit. (1) and the injection pump (2). Hydrothermal liquefaction biomass treatment device according to claim 1, characterized in that it comprises, downstream of the electrolyser (9), a connection to the hydrothermal liquefaction reactor (3). 4. Device for treating biomass by hydrothermal liquefaction according to one of claims 1 to 3, characterized in that it further comprises a settling unit (10) downstream of the electrolyser (9). Process for transforming biomass comprising the following steps in the device according to one of the claims. 1 to 4: preparation of a fluid by mixing biomass with water; injecting this fluid into a hydrothermal liquefaction reactor; transformation of the biomass in the hydrothermal liquefaction reactor; obtaining a fluid comprising oil, the tank, gases, an aqueous phase containing oxygenated compounds; separation of the oil, the tank, the t of the aqueous phase containing oxygenated compounds; 3035404 - formation of hydrocarbons by electrolysis of the aqueous phase containing oxygenated compounds. Process for transforming biomass according to Claim 5, characterized in that the oxygenated compounds of the aqueous phase are ketones, phenolic compounds and carboxylic acids. Process for transforming biomass according to claim 5 or 6, characterized in that the electrolytically formed hydrocarbons are separated from the aqueous phase. by settling. Process for transforming biomass according to one of Claims 5 to 7, characterized in that the electrolyzed aqueous phase is used to prepare the fluid injected into the hydrothermal liquefaction reactor. Process for transforming biomass according to one of Claims 5 to 5. at 8, characterized in that the fluid injected into the hydrothermal liquefaction reactor has a basic pH, advantageously between 8 and 10. Process for transforming the biomass according to one of Claims 5 to 9, characterized in that csi electrolysis carried out at a temperature between 20 and 60 ° C by application of a voltage of between 1 and 10 V.
    类似技术:
    公开号 | 公开日 | 专利标题
    EP3286284B1|2019-06-05|Device and method for treating biomass
    EP2668250B1|2019-04-24|Production of fuel from chemicals derived from biomass
    US8183421B2|2012-05-22|Biofuel production by high temperature non-faradaic electrochemical modification of catalysis
    CN102471903B|2015-03-11|Decarboxylation cell for production of coupled radical products
    EA019492B1|2014-04-30|A method for digesting a biomass comprising lignin together with cellulose and/or hemicellulose
    CN101044089A|2007-09-26|Base-facilitated production of hydrogen from biomass
    RU2014118837A|2015-11-20|METHOD AND SYSTEM FOR PROCESSING CARBON-CONTAINING GASES BY ELECTROCHEMICAL HYDROGENIZATION FOR PRODUCING CxHyOz COMPOUND
    CN104073278A|2014-10-01|Method for converting lignin into liquid fuel through adopting two-step method
    WO2011149079A1|2011-12-01|Hybrid thermal power generation system and method for constructing same
    JP2004124008A|2004-04-22|Preparation process of vegetable oil fuel
    Wu et al.2020|Near complete valorisation of Hybrid pennisetum to biomethane and lignin nanoparticles based on gamma-valerolactone/water pretreatment
    FR3053048B1|2019-08-23|COMBUSTIBLE COMPOSITION FROM BIOMASS AND PROCESS FOR PREPARING THE SAME
    Yan et al.2019|Solar Thermal Electrochemical Process | action to biomass: Solar thermo-coupled electrochemical synergy for efficient breaking of biomass to biofuels and hydrogen
    EP2836457A1|2015-02-18|Production of dihydrogen by means of the conversion of top gases originating from a synthesis step
    CN103980929B|2015-06-24|Method for preparing biological fuel oil by fast pyrolyzing biomass
    CN110713853B|2021-09-10|Method for utilizing oily wastewater by combining electro-catalysis with algae
    CA2908125A1|2014-10-23|Method for producing hydrocarbides
    EP3083547B1|2018-09-05|Method for separating mandelic compounds in salified form and use of same for preparing aromatic aldehyde
    US10934242B2|2021-03-02|Electrochemical method for producing valeric acid
    EP3643766B1|2021-04-28|Method for refining bio-oil from pyrolysis
    CN108676818B|2021-06-01|Method for quickly converting organic waste into energy
    BE1016600A6|2007-02-06|Treatment of liquid effluents and/or sludge, useful to prepare a solid product, which is useful in agriculture, comprises electrolysis and biomethanation of the liquid effluents and/or the sludge
    KR20100074172A|2010-07-01|Production of fatty acid and fatty acid ester
    EP2134645B1|2019-11-13|Method for producing medium to long-chained hydrocarbons
    Garedew et al.2013|Pyrolysis and electrocatalysis of extractive ammonia-processed lignin to increase the value of sugar-platform based bioenergy systems
    同族专利:
    公开号 | 公开日
    FR3035404B1|2019-04-05|
    WO2016169927A1|2016-10-27|
    EP3286284B1|2019-06-05|
    EP3286284A1|2018-02-28|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US20140273141A1|2013-03-14|2014-09-18|Algae Systems, LLC|Integrated Biorefinery|
    CN106673389A|2017-01-24|2017-05-17|中国农业大学|Heat-treatment recycling method for excrement|
    IT201800007569A1|2018-07-27|2020-01-27|Eni Spa|PROCEDURE FOR THE PRODUCTION OF BIO-OIL AND BIOGAS STARTING FROM BIOMASS|
    CN110713853B|2019-10-24|2021-09-10|江苏大学|Method for utilizing oily wastewater by combining electro-catalysis with algae|
    WO2021121526A1|2019-12-20|2021-06-24|Ib Johannsen|Cost efficient integration of hydrothermal liquefaction and wet oxidation wastewater treatment.|
    法律状态:
    2016-04-28| PLFP| Fee payment|Year of fee payment: 2 |
    2016-10-28| PLSC| Search report ready|Effective date: 20161028 |
    2017-04-28| PLFP| Fee payment|Year of fee payment: 3 |
    2018-04-26| PLFP| Fee payment|Year of fee payment: 4 |
    2019-04-29| PLFP| Fee payment|Year of fee payment: 5 |
    2020-04-30| PLFP| Fee payment|Year of fee payment: 6 |
    2021-04-29| PLFP| Fee payment|Year of fee payment: 7 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1553601A|FR3035404B1|2015-04-22|2015-04-22|DEVICE AND METHOD FOR TREATING BIOMASS|
    FR1553601|2015-04-22|FR1553601A| FR3035404B1|2015-04-22|2015-04-22|DEVICE AND METHOD FOR TREATING BIOMASS|
    EP16721670.4A| EP3286284B1|2015-04-22|2016-04-19|Device and method for treating biomass|
    PCT/EP2016/058650| WO2016169927A1|2015-04-22|2016-04-19|Device and method for treating biomass|
    [返回顶部]