WO2011047696A1 - Procédé de conversion de la biomasse et dispositif associé - Google Patents

Procédé de conversion de la biomasse et dispositif associé Download PDF

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Publication number
WO2011047696A1
WO2011047696A1 PCT/EP2009/007534 EP2009007534W WO2011047696A1 WO 2011047696 A1 WO2011047696 A1 WO 2011047696A1 EP 2009007534 W EP2009007534 W EP 2009007534W WO 2011047696 A1 WO2011047696 A1 WO 2011047696A1
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WO
WIPO (PCT)
Prior art keywords
reactor
biomass
jacket
pressure reactor
pressure
Prior art date
Application number
PCT/EP2009/007534
Other languages
German (de)
English (en)
Inventor
Hans-Gerd RÜCKER
Nic Haagen
Oliver Weiss
Original Assignee
Bioethika Umwelttechnologien Ag
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Filing date
Publication date
Application filed by Bioethika Umwelttechnologien Ag filed Critical Bioethika Umwelttechnologien Ag
Priority to PCT/EP2009/007534 priority Critical patent/WO2011047696A1/fr
Publication of WO2011047696A1 publication Critical patent/WO2011047696A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/04—Pressure vessels, e.g. autoclaves
    • B01J3/042—Pressure vessels, e.g. autoclaves in the form of a tube
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/60—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis
    • B01F27/72—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with helices or sections of helices
    • B01F27/725—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with helices or sections of helices with two or more helices in respective separate casings, e.g. one casing inside the other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms 
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/82—Combinations of dissimilar mixers
    • B01F33/821—Combinations of dissimilar mixers with consecutive receptacles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/90—Heating or cooling systems
    • B01F35/92—Heating or cooling systems for heating the outside of the receptacle, e.g. heated jackets or burners
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1812—Tubular reactors
    • B01J19/1843—Concentric tube
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/20—Stationary reactors having moving elements inside in the form of helices, e.g. screw reactors
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/44—Solid fuels essentially based on materials of non-mineral origin on vegetable substances
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/46—Solid fuels essentially based on materials of non-mineral origin on sewage, house, or town refuse
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/48—Solid fuels essentially based on materials of non-mineral origin on industrial residues and waste materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C10L9/086—Hydrothermal carbonization
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/182—Details relating to the spatial orientation of the reactor horizontal
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention relates to a process for the conversion of biomass of municipal, agricultural and / or industrial origin into carbonaceous substances of other composition, in which the biomass is mixed with water, the water-containing biomass is added to a catalyst, the water-and catalyst-enriched biomass in a pressure reactor a thermal reaction under pressure, exclusion of air and dehydration is subjected.
  • the invention relates to a device for carrying out the method.
  • a method of the type mentioned is given in DE 196 31 201 C2.
  • a disadvantage of the known method is that the heating of the biomass takes place within the pressure reactor with the aid of an external heat source, in the present case via generators for generating microwave radiation. The process is energy intensive and therefore not economically efficient.
  • CONFIRMATION COPY It is known to produce fuels by means of so-called hydrothermal carbonization ("coalification") from biomass with the release of heat energy.
  • hydrothermal carbonization hydrothermal carbonization
  • EP 1 970 431 AI, WO 2008/113309 AI, DE 10 2007 022 840 AI invoke the already explored in 1913 by Friedrich Bergius chemical process, without mentioning any further prior art concretely.
  • the biomass consisting of biowaste, grass, leaves and other plant residues is slurried with water, treated with a catalyst such as citric acid and transferred in a pressure reactor under elevated temperature and pressure over a few conversion stages emission-free in a carbonaceous material. There will be no carbon dioxide released during the process.
  • a device for the carbonization of organic substances shows DE 34 24 373 AI.
  • the device consists of a pressure chamber, called carburizing chamber, whose one wall is arranged displaceable so that the waste can be continuously compressed.
  • the compressive forces are to be increased during compression until the resulting from these forces molecular friction in the organic matter, which are located in the Kolohlungshunt, has generated so much heat that under the simultaneous action of pressure and heat, while approximately exclusion of Oxygen, these organic substances are subjected to a coalification.
  • EP 0 204 354 B1 describes a process for the production of hydrocarbons containing liquids from biomass, in which the biomass is brought into a reaction zone at elevated temperature and pressure.
  • EP 0 052 334 B2 discloses a device for obtaining solid, liquid and gaseous fuels from organic material, therein sewage sludge, in which within a heated reactor tube a screw conveyor is arranged.
  • biomass is heated under exclusion of air to a temperature of 200 to 600 degrees Celsius, but without the involvement of reduction and oxidation processes.
  • This object is achieved by a generic method in which the biomass is preheated before and after the occurrence of the thermal reaction outside the pressure reactor and is supplied to the pressure reactor in the preheated state, the reaction in the pressure reactor is initiated by the preheated and catalyst-enriched biomass, the biomass continuously passes the pressure reactor, wherein the preheated part of the biomass is surrounded by another part of the biomass located in the pressure reactor.
  • Biomass is understood to mean an organic material which is preferably biological, water-containing residues and waste. These materials usually come from households (biowaste), from industrial plants (breweries, Food processing, paper mills, pharmaceutical industry etc) and as sewage sludge biological wastewater treatment. The materials also include agricultural and forestry waste and the remainder of renewable raw materials containing cellulose. The biomass can also be added to wood and wood-based panels if they have been shredded accordingly beforehand.
  • the reaction proceeds in the presence of at least one acidic catalyst and is exothermic.
  • the catalyst used is citric acid, which reacts with the cellulosic material of the biomass.
  • citric acid and other organic acids such as acetic, formic, succinic, tartaric u. a., in question.
  • the biomass passes through the pressure reactor at least at predetermined time intervals in opposite directions of flow. It is particularly advantageous to put the biomass at the same time in a rotational movement, which can be done in one or simultaneously in two opposite directions of rotation. These measures improve the heat exchange of the biomass streams.
  • the preheating of the biomass outside the pressure reactor can take place in a heatable mixing container.
  • the biomass can be preheated to a temperature of up to about 200 ° C., preferably it should be preheated between 95 ° C. and 135 ° C. It is advantageous that the preheating of the biomass in the mixing vessel is assisted by the waste heat obtained from the pressure reactor.
  • start-up phase At the beginning of the process, called start-up phase, at least part of the biomass in the pressure reactor is heated by at least one external heat source, such as the heating cartridge.
  • the warm-up cartridges may be placed at multiple locations of the indoor and / or outdoor reactor. Otherwise the process runs without power from the outside, so that it can be run independently after the start-up phase.
  • the process is continuous, as if in a cycle where new material (biomass) can be fed in and processed material (product) can be removed again and again. Due to the exothermic reaction, excess energy is generated which, in the form of steam, can drive at least one steam engine with an electric generator.
  • the advantage is that apart from the start-up phase no heat must be supplied from the outside and that the heat-related fluctuations of the process can be compensated thanks to the available energy surplus.
  • the output of the processed mass from the pressure reactor can be made in stages by successively opening and closing several drain valves. This gives carbonaceous products of varying consistency and density.
  • An apparatus for carrying out the method consists essentially of the following listed parts: at least one pressure reactor, which consists of an outer reactor and at least one inner reactor, and at least one, the inner reactor upstream, heatable mixing vessel.
  • both the inner reactor and the outer reactor are cylindrical, the two having a common Have longitudinal axis, so that an uninterrupted tube in-tube arrangement arises.
  • the inner reactor is rotatably arranged with respect to the outer reactor, wherein the rotational movement can be realized in one or in two opposite directions of rotation about said longitudinal axis.
  • cylindrical inner reactor may be provided with an inner screw and / or with an outer screw.
  • the internal screw can be arranged rotatably with respect to a jacket of the internal reactor or rigidly connected to a jacket inside the rotatable internal reactor.
  • the inner screw or outer screw several separate stirring arms can be used.
  • the mixing container may be equipped with at least one agitator whose drive axis is vertical, d. H. can be arranged perpendicular to the longitudinal axis of the pressure reactor or horizontally or inclined. It is important that the mixing vessel, as well as the pressure reactor is made airtight and thermally insulated in order to minimize the heat losses.
  • the pressure reactor can rest on a suitably solidified substrate, for example on a concrete floor or a platform lying above the ground. It is conceivable to set up the entire device or at least the pressure reactor for the purpose of mobility of the system on a vehicle platform.
  • the device works emission-free and binds C0 2 and CO.
  • the products resulting from metabolism can be used as required used for energy production or as a soil conditioner and fertilizer.
  • FIG. 1 shows a pressure reactor with connected mixing container, in a schematic side view
  • Fig. 2 shows the pressure reactor of FIG. 1 in a schematic
  • FIG. 3 shows the pressure reactor according to FIG. 1 in a longitudinal section
  • FIG. 5 shows the pressure reactor of FIG. 1 in an enlarged
  • Fig. 6 shows a detail "C" according to Fig.l
  • Fig. 7 is a schematic division of the outer reactor in
  • the device 100 shown in FIG. 4 or plant consists essentially of a pressure reactor 2 with two connected mixing vessels 1.1 and 1.2, a steam boiler 16, two power generators 17, a condensation water tank 19, a reagent tank 20, a heater 21 and a collecting container 22.
  • the steam boiler 16 is connected via a line 30 and a pressure relief valve 18 to the pressure reactor 2.
  • the pressure reactor 2 is shown in detail in FIGS. 3 and 5. It consists of a cylindrical outer reactor 2.2 and an nem also cylindrical inner reactor 2.1 together.
  • the outer reactor 2.2 has a jacket 9 and two end walls 31.1 and 31.2, on which the inner reactor 2.1 is mounted.
  • the inner reactor 2.1 in turn has a jacket 3 which is longer than the jacket 9 of the outer reactor.
  • the outer reactor 2.2 has a chamber 39 whose effective volume is limited by the jacket 9 and by the inner reactor 2.1 and by the outer screw 5.
  • the inner reactor 2.1 or its jacket 3 is rotatably disposed within the outer reactor 2.2.
  • an inner screw 4 which is rotatable about a shaft 25 and extends almost as far as a casing inner side 32, runs. H. it slides during the rotational movement over the jacket-inner side 32. The rotational movement of the inner screw 4 is reversible.
  • the jacket 3 of the inner reactor 2.1 is of an outer screw
  • the mixing container 1 is through a cylindrical double jacket
  • the mixing container 1 tapers conically downward and closes via a controlled Ven- til 23 (flap) to a filling opening 34 of the inner reactor 2.1 at.
  • the mixing container 1 and the inner reactor 2.1 including inner and outer screws are made of a bronze alloy.
  • the jacket 9 and end walls 31.1, 31.2 of the outer reactor 2.2 are made of a corrosion-resistant steel alloy and vacuum-insulated similar to the mixing container 1.
  • the inner reactor 2.1 On the jacket 3 of the inner reactor 2.1, two closable outlets 10.1, 10.2 are provided (cf., Fig. 5), of which the outlet 10.1 leads directly into the outer reactor 2.2.
  • the second outlet 10.2 is connectable to a collecting container 22. This allows the discharge of the product located in the inner tube either in the outer reactor 2.2 or in the collecting container.
  • the inner reactor 2.1 is provided at its end facing away from the mixing container 35 with a hydraulic piston 11, by means of which a drain valve 36 can close and open the arranged on the jacket 3 outlet 10.1.
  • a discharge opening 14.1 is arranged for discharging the finished product.
  • An additional discharge opening 14.2 is located immediately in front of the rear end wall 31.1.
  • the pressure reactor 2 is equipped with conventional fittings, such as thermometer 26, pressure gauge 27, pH meter 28 and sampling point 29.
  • the parts of the fitting are each provided at several points of the shell 9.
  • FIG. 7 Each field shown schematically in Fig. 7 corresponds to a volume V2 of the inner reactor 2.1; This results in a total volume V3 of the outer reactor:
  • V3 9 x V2
  • the volume V2 of the inner reactor should not be exceeded by a volume VI of the mixing container, d. H.
  • the boiler pressure in the steam boiler 16 should be between 18 and 20 bar;
  • the PJ value of the dry matter is on average 17,000 kJ / kg;
  • the residence time of the biomass in the inner reactor is about 1 hour.
  • the warming cartridges 15.1, 15.2 heated to about 170 ° C. with thermal oil are introduced into the empty pressure reactor 2.
  • the heating cartridges are made of bronze alloy and each have a volume of about 0.7 m 3 .
  • the warming cartridges are made of bronze alloy and each have a volume of about 0.7 m 3 .
  • 15.1, 15.2 are accommodated in an inlet 37 (see Fig. 7) of the inner reactor 2.1 and at the opposite end of the outer reactor 2.2 at its end 31.1 (see Fig. 7) or via the outlet 14.2 shown in Fig. 5 in the outer reactor.
  • the number and arrangement of the heating cartridges 15.1, 15.2 am Pressure reactor is chosen only as an example and can be made differently if required.
  • Biomass and about 15% by weight of water are pumped into two mixing vessels 1.1, 1.2 (see FIG. 4) via the inlet connection 13 on the cover 12 until the mixing vessels are filled. With the agitator 24, the mixture is processed to a homogeneous mass.
  • the excess of preheated biomass in both mixing vessels 1.1, 1.2 is sufficient for the filling of the inner reactor 2.1 and for portionwise charging of the outer reactor.
  • a field 38 corresponds to the volume V2 of the inner reactor (see Fig. 7).
  • the portions of the biomass in the present case 9 portions will pass from the inner reactor 2.1 gradually into the chamber 39 of the outer reactor 2.2 via the outlet 10.1 (left side Fig.5), which is opened by means of hydraulic piston 11 and draining slide 36 each time , This ensures that the mass in the chamber 39 is not mixed with each other and the calorific value of the mass located in a field can be fully utilized.
  • the process, which is carried out under exclusion of air, is continuous and can take months as required.
  • the residence time of the predetermined amount of biomass in the inner reactor 2.1 is about 1 hour, d. H. Each hour, another portion of the preheated biomass is fed from the mixing vessel into the inner reactor without having to stop the process.
  • the inner screw 4 turns left and right and thereby homogenizes the mass.
  • the mass is discharged from the inner reactor in the flow direction Rl via the outlet 10.1 in the outer reactor 2.2 and at the same time a reagent, here: citric acid and water supplied from the reagent tank 20, wherein the weight ratio of water to reactant is about 20.
  • the reactant initiates the exothermic process already at a temperature of 170 ° C, which produces water vapor.
  • a temperature of 210 ° C creates an overpressure of 20 bar.
  • the generated steam also has a pressure of 20 bar.
  • the water is supplied in mist form in order to achieve the greatest total surface area.
  • the mass moves around a field in the flow direction R2 and after 9 hours it reaches the last field where the outlet 14.2 is.
  • the processed mass is discharged and the first field is filled with the mass from the inner reactor 2.1 via the outlet 10.1.
  • the inner reactor is again filled with the pre-heated in the mixing container 1.1 or 1.2 mass and mixed.
  • the biomass in the outer reactor lingers for about 9 hours at a temperature between 200 and 210 ° C until the calorific value of the mass is used up.
  • the outlet of the mass is carried out in two stages as needed.
  • the outlets 14.1, 14.2 (drain valves) on the outer reactor are then opened sequentially, so that no air enters the process.
  • the rotational movement of the outer screw 5 is set or a very slow rotation of the outer screw and thus of the shell 3 is made.
  • the steam passes via the pressure relief valve 18 and thermo-insulated line 30 into the steam boiler 16, to which two power generators 17 connected in series are connected.
  • the rest of the electricity is fed into the public grid.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention a pour objet un procédé de conversion de la biomasse d'origine municipale, agricole et/ou industrielle en matières carbonées d'une autre composition. La biomasse est préchauffée avant et après la survenue de la réaction thermique à l'extérieur du réacteur sous pression, la réaction dans le réacteur sous pression étant initiée par la biomasse préchauffée et enrichie à l'aide d'un catalyseur, et la biomasse traversant en continu le réacteur sous pression, du fait que la partie préchauffée de la biomasse est entourée par une partie restante de la biomasse qui se trouve dans le réacteur sous pression. La présente invention concerne également un dispositif pour la mise en œuvre du procédé comprenant au moins un réacteur sous pression (2), qui est composé d'au moins un réacteur interne (2.1) et d'un réacteur externe (2.2), le réacteur externe étant pourvu d'au moins une ouverture d'évacuation (14.1, 14.2). Au moins un récipient de mélange chauffant (1) se trouve en amont du réacteur interne. Une vis externe (5) est disposée sur une gaine (3) du réacteur interne et une vis interne (4) est disposée à l'intérieur du réacteur interne. Les vis interne et externe (4; 5) peuvent pivoter de manière réversible.
PCT/EP2009/007534 2009-10-21 2009-10-21 Procédé de conversion de la biomasse et dispositif associé WO2011047696A1 (fr)

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PCT/EP2009/007534 WO2011047696A1 (fr) 2009-10-21 2009-10-21 Procédé de conversion de la biomasse et dispositif associé

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013124414A3 (fr) * 2012-02-24 2013-10-24 Nk New Knowledge Ag Cuve de carbonisation pour carbonisation hydrothermale
ES2441318A1 (es) * 2012-07-31 2014-02-03 Ingelia, S.L. Proceso de bombeo de biomasa en un proceso de carbonización hidrotermal
WO2014145731A1 (fr) * 2013-03-15 2014-09-18 Gas Technology Institute Production rapide d'une biomasse carbonisée hydrothermiquement par extrusion réactive à deux vis
CN105413534A (zh) * 2015-11-25 2016-03-23 郑臣钏 一种高效化工混合装置

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008095589A1 (fr) * 2007-02-08 2008-08-14 Grenol GmbH Carbonisation hydrothermique de biomasse
DE102007022840A1 (de) * 2007-05-11 2008-12-24 Suncoal Industries Gmbh Verfahren zur Kühlung und Vorwärmung einer Anlage zur hydrothermalen Carbonisierung von Biomasse
EP2166061A1 (fr) * 2008-09-18 2010-03-24 Artes Biotechnology GmbH Dispositif et procédé destinés au traitement de biomasse
WO2010092040A1 (fr) * 2009-02-10 2010-08-19 Csl Carbon Solutions Ltd. Procédé hydrothermal pour la préparation d'un matériau de type charbon à partir d'une biomasse et colonne d'évaporation

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008095589A1 (fr) * 2007-02-08 2008-08-14 Grenol GmbH Carbonisation hydrothermique de biomasse
DE102007022840A1 (de) * 2007-05-11 2008-12-24 Suncoal Industries Gmbh Verfahren zur Kühlung und Vorwärmung einer Anlage zur hydrothermalen Carbonisierung von Biomasse
EP2166061A1 (fr) * 2008-09-18 2010-03-24 Artes Biotechnology GmbH Dispositif et procédé destinés au traitement de biomasse
WO2010092040A1 (fr) * 2009-02-10 2010-08-19 Csl Carbon Solutions Ltd. Procédé hydrothermal pour la préparation d'un matériau de type charbon à partir d'une biomasse et colonne d'évaporation

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013124414A3 (fr) * 2012-02-24 2013-10-24 Nk New Knowledge Ag Cuve de carbonisation pour carbonisation hydrothermale
ES2441318A1 (es) * 2012-07-31 2014-02-03 Ingelia, S.L. Proceso de bombeo de biomasa en un proceso de carbonización hidrotermal
WO2014145731A1 (fr) * 2013-03-15 2014-09-18 Gas Technology Institute Production rapide d'une biomasse carbonisée hydrothermiquement par extrusion réactive à deux vis
US10442995B2 (en) 2013-03-15 2019-10-15 Gas Technology Institute Rapid production of hydrothermally carbonized biomass via reactive twin-screw extrusion
CN105413534A (zh) * 2015-11-25 2016-03-23 郑臣钏 一种高效化工混合装置

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