WO2012110325A1 - Procédé et réacteur de carbonisation hydrothermale de la biomasse - Google Patents

Procédé et réacteur de carbonisation hydrothermale de la biomasse Download PDF

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Publication number
WO2012110325A1
WO2012110325A1 PCT/EP2012/051824 EP2012051824W WO2012110325A1 WO 2012110325 A1 WO2012110325 A1 WO 2012110325A1 EP 2012051824 W EP2012051824 W EP 2012051824W WO 2012110325 A1 WO2012110325 A1 WO 2012110325A1
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WO
WIPO (PCT)
Prior art keywords
reactor
reaction
power plant
reaction products
biomass
Prior art date
Application number
PCT/EP2012/051824
Other languages
German (de)
English (en)
Inventor
Bernd Utz
Marco Dornauer
Original Assignee
Siemens Aktiengesellschaft
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 Siemens Aktiengesellschaft filed Critical Siemens Aktiengesellschaft
Publication of WO2012110325A1 publication Critical patent/WO2012110325A1/fr

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Classifications

    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to a method for
  • hydrothermal carbonization in which biomass is fed into a reactor and excited to a chemical reaction and then reaction products are removed from the reactor. It also relates to a reactor for such hydrothermal carbonization of biomass.
  • Hydrothermal carbonation is a chemical process for the simple and efficient production of
  • Reaction products such as lignite, synthesis gas, liquid petroleum precursors and humus or peat from biomass under
  • Biomass 3 is first crushed in a treatment tank 6 and together with reaction water 5 and a reaction support means 7, namely a
  • Catalyst here citric acid, placed in a reactor 1.
  • heat ⁇ ⁇ is supplied, whereby an endothermic reaction is initiated.
  • Gases 9, such as CO 2 and water vapor are removed during the process.
  • About a pipe 11 is this
  • a mechanical drying here by centrifuging
  • the final reaction product 29 is a dry, granular, lignite-like substance.
  • the biomass 3 is in particular to
  • the reactor 1 is a pressure vessel whose
  • the reaction produces not only waste heat AT out , but also a significantly increased pressure, which can be up to 2 MPA.
  • oxonium ions are formed which lower the pH to 5 and below. This effect can be anticipated by adding reaction promoting agents such as citric acid 7 as a catalyst. It should be noted that the lower the pH, the more
  • Brown coal spheres (formula C 6 H 2 O) with pore sizes between 8 and 20 nm are present as a solid phase. The remaining 1 to 10% of the carbon is either dissolved in the aqueous phase or converted to carbon dioxide.
  • the reaction liberates 1105 kJ of energy per mole.
  • Carbonation is a smaller scale application because the process is difficult to control and requires many preparatory steps such as coarse sorting and size reduction as well as post-processing steps (especially drying and reactor 1 purification).
  • the process currently proves to be relatively cumbersome, since in each case for filling and emptying and cleaning of the reactor 1 working rush hours arise, while then incurred in the entire course of the 12 hours of the reaction hardly any further work.
  • the process can only be automated inadequately.
  • the object of the invention is therefore to enable an improved, in particular preferred, a process simplified in the course of hydrothermal carbonization and to provide the corresponding working means therefor.
  • Another optional object of the invention is to effectively reuse the resulting reaction products.
  • Waste heat generated during the phase of the exothermic reaction for heating in the context of a parallel endothermic reaction in the context of a return
  • Procedure also requires that the reactor does not have to be switched on and off again and again, but can be operated constantly, and the peak times of the workload for the operation of the reactor can be at least reduced. In other words, both the working and the
  • Vegetable material is preferably used as biomass, but it is also possible to use animal substances or other biological material, for example fungi. Furthermore, the term biomass in the
  • Hydrocarbon compounds such as polyethylene.
  • such substances can also be used in the context of the process since they too can be converted into similar or identical reaction products as the biomass generated from biological processes.
  • the process according to the invention is carried out in a pre-reactor, in which also carried out an initial reaction becomes.
  • the pre-reactor is spatially separated at least during the feed from a main reactor in which an exothermic chemical reaction is carried out.
  • the reactor is thus in at least two different
  • Subdivided reaction chambers of which the first, namely the pre-reactor, is used as an atrium.
  • the pressure built up in the prereactor in the course of the reaction and the temperature achieved there can be transferred to the main reactor, so that the pressure and temperature conditions are essentially the same in both reactor parts.
  • Partial processes are: The loading of the reactor with biomass, the initial endothermic reaction, the exothermic reaction and the discharge of the reactor. So it's possible
  • Reaction products are preferably controlled by a suitable control device, which particularly preferably derives control commands for at least one of these two processes from a time control and / or from user commands. This can ensure that the reactor
  • the biomass is heated in the prereactor and
  • the pre-reactor serves to initiate the reaction of the hydrothermal carbonization, that is, the biomass on a
  • the pre-reactor is the part of the reactor in which the carbonation reaction is initiated until it becomes self-contained
  • the target pH may be considered to be pH 5 and below.
  • Reaction water which in particular during the reaction in the pre-reactor acts as a carrier and transfer agent and on the other hand, catalysts or acids, such as the above-mentioned citric acid, which serve to reduce the pH.
  • catalysts or acids such as the above-mentioned citric acid
  • reaction intermediates formed in the respective partial reactors can be forwarded to the next partial reactor by utilizing gravity.
  • the partial reactors are temporarily separated from one another, which means that individual reaction steps take place in the partial reactors, without any connection to the other partial reactors.
  • the result is that in each of the sub-reactors a separate category of reaction intermediate (or fraction) can be prepared separately and then, if necessary, after expiration of one of these
  • the main reactor comprises at least three partial reactors, more preferably even four partial reactors.
  • the increase in the number of partial reactors can lead to a differentiation of the reaction process in that very different
  • Reaction products can be produced and removed if necessary.
  • the increase in the number of sub-reactors can also be used to optimize the timing of the process: it takes about eight hours to form peat, while only four hours are required to then produce lignite from this. It may therefore be advantageous to use two sub-reactors, with only the second complete peat being present, while the piling process is only begun in the first of the two sub-reactors.
  • the intermediate reaction product is then passed from the first peat-part reactor to the second peat-part reactor, and after a further four hours, passed into another partial reactor in which lignite is produced. This results in a clocking of four hours, compared to a clock of eight hours, when peat in one
  • the reactor is preferably equipped or connected to a control device which, in operation, depends on a (reaction) given in accordance with a rule.
  • recovered intermediate reaction products are preferably from the prereactor in the main reactor and / or from one part-reactor to a next part-reactor via sluices and / or
  • Valves forwarded Such locks, such as rotary valves, or such valves are used, controlled and possibly differentiated metered the biomass
  • lignite or coal-like substances from the end-part reactor intermediate reaction products such as petroleum precursors, humus, or lignite-like substances are removed from a partial reactor, which is arranged in the main reactor in the process direction before the end-part reactor.
  • This part-reactor, which supplies lignite-like substances, is according to a preferred
  • the end-part reactor or, in other words, in the end-part reactor, the reaction is continued until the presence of brown coal-like products.
  • Reaction products in a sufficiently high concentration thus requires a functional separation of the partial reactors from each other.
  • the first part-reactor acts as a "crude oil precursor reactor”
  • the second part-reactor as a "humus reactor”
  • the third part-reactor as a "brown coal reactor”.
  • Such a designation and functional assignment can advantageously be displayed directly on the outside of the respective sub-reactors in order to present even unknowable users, which products can be obtained from the respective sub-reactor after expiration of the reaction time provided for this purpose.
  • reaction products from the method according to the invention for firing a power plant for the generation of electric power are forwarded.
  • Reaction products can be directly via piping
  • a reactor according to the invention is therefore preferably developed in such a way that it has a compound for the transmission of the reaction products to a power plant for the production of
  • reaction products includes electric power, so that the reaction products can continue to be used for firing the power plant.
  • a compound is in effect a transport compound for the reaction products and can be both standing
  • Connection for example in the form of a pipeline to be realized as well as a temporary transport connection, for example, realized by other terrestrial means of transport.
  • Such means of transport may include, inter alia Trains or trucks act on a Schienenpositioned. Road connection from the reactor to the power station.
  • reaction products from the inventive method for supporting firing in a heating circuit in particular in a solar thermal power plant.
  • a heating circuit in particular in a solar thermal power plant.
  • solar thermal power plants require a so-called back-up firing, which is mainly used when not enough heat through
  • the end effect is thus a cycle in which a local solar thermal power plant, supported by
  • Agriculture provides energy that in turn can be used in whole or in part to support local agricultural cultivation.
  • the invention thus also includes a power plant, in particular a solar thermal power plant comprising a
  • Main heat energy source is preferably a solar panel with a number of solar panels
  • Solar radiation generate heat. This heat is then used in a heating circuit to directly or indirectly drive a turbine to generate electricity.
  • the reactor and the power plant are subunits of a production plant, which are preferably arranged on a common operating area. This results in very short connections; a simple control of the processes, in particular the
  • the invention comprises a method for operating a power plant, preferably a solar thermal
  • Process produced reaction used for firing power station.
  • coal-like reaction products ie lignite or coal-carbon reaction products
  • These reaction products have a particularly high calorific value; their drying out of the aqueous solution can also be achieved by using residual heat from the reaction process or from the heating and / or
  • Figure 2 is a schematic block diagram of a
  • Figure 3 is a schematic block diagram of a
  • Embodiment of a power plant reactor complex according to the invention Embodiment of a power plant reactor complex according to the invention.
  • FIG 2 shows an embodiment of a reactor according to the invention 1 'with a pre-reactor 17 and a main reactor 19, which are connected to each other via a lock 21.
  • biomass in particular vegetable biomass, together with water of reaction 5 and citric acid 7 is fed.
  • the biomass 3 is, as already explained in connection with Figure 1, crushed.
  • the main reactor 19 is divided into n sub-reactors 25a, 25b, 25c, 25d, ..., 25n.
  • the main reactor 19 is followed by the endothermic reaction independent running exothermic Karbonmaschinesrepress of related from the prereactor 17 mixture with release of exhaust gases 22, namely carbon dioxide and steam.
  • a reaction can take place in the first part-reactor 25a, as a result of which
  • aqueous petroleum precursor is present.
  • the reaction can continue until a second one
  • the reaction is carried out to a third intermediate product 29c, such as a lignite-like substance, and in the fourth partial reactor 25d, the mixture reacts further until the
  • a fourth intermediate or final product 29d for example in the form of a charcoal-like substance. All the mentioned intermediate or end products 29a, 29b, 29c, 29d are mixed with the water of reaction or the water which is deposited during the reaction. In total, an intermediate or end product 29a, 29b, 29c, 29d, 29n can be obtained in each of the n partial reactors 25a, 25b, 25c, 25d,... 25n.
  • An end product 29n may be, for example
  • the sub-reactors 25a, 25b, 25c, 25d, 25n are arranged in the order of their mention from top to bottom and separated by separators 24a, 24b, 24c, 24n. Via valves 23a, 23b, 23c, 23n, the intermediate and final reaction products 29a, 29b, 29c, 29d, 29n can be introduced both into the respective next sub-reactor 25b, 25c, 25d, 25n
  • control commands SB which consists of a
  • Control unit 26 are related. This control unit 26 receives user commands NB and Timing commands Tim via suitable interfaces (not shown) to go to the right
  • the user commands NB refer to a reference request for certain
  • Reaction products 29a, 29b, 29c, 29d, 29n may each according to current product needs, for example a need for humus 29b for fertilizing fields.
  • FIG. 3 A particularly preferred application of the reactor 1 'according to the invention is shown in FIG. 3 for use in a power plant-reactor complex 65.
  • the reactor 1 ' is disposed within a reactor complex 61 and
  • Reactor complex 61 comprises in addition to the reactor 1 'a
  • Preparation tank 6 a first dryer 31, a second dryer 33 (see Figure 1), a silo 35 and a connection 36 in the direction of the power plant 63, which is realized as a supply line in the power plant 63.
  • the product dried in this way for example brown or hard coal in the form of granules, is collected and stored in the silo 35 and, if necessary, passed on to the power plant 63 via the line connection 36.
  • the power plant 63 comprises a solar field 39 with a plurality of solar panels, which is arranged in a cardiovascular 45.
  • a carrier medium, here oil, is circulated in the heating circuit 45 via a pump 43, heated in the solar field 39 and
  • the temperature of the oil is used to make water in one
  • Operating cycle 47 to heat so that it produces water vapor.
  • the operating circuit 47 is operated by means of a second pump 49, so that after passing through the
  • Evaporator 41 generated steam drives a turbine 53, which in turn operates a generator 55.
  • Generator 55 generates from the rotational energy of the turbine 53 electricity.
  • a condenser 51 which is connected to a cooling tower 57, the water vapor is cooled again to a lower temperature, so that in
  • the Stauerakiung 37 serves to provide the additional heating power that can not be provided by the irradiation of the sun 59 to the solar panel 39 at a certain time. This is the case, for example, when the sun is cloudy or at dusk or night. In such cases, the Stauer85ung 37 wholly or partially assumes the function of heat generation to ensure the necessary operating temperature of the heating circuit 45.
  • the power plant-reactor complex 65 is located on an area on which the reactor complex 61 and the power plant 63 are located in common. This results in a direct feed of the biomass 3 obtained
  • Reaction products 29 in the power plant 63 The electrical energy that can be obtained from the power plant 63, in the sequence, for example, for the operation

Abstract

L'invention concerne un procédé de carbonisation hydrothermale, selon lequel la biomasse (3) est introduite dans un réacteur (1') et est soumise à une réaction chimique, après quoi les produits de la réaction (13, 15, 29, 29a, 29b, 29c, 29d,..., 29n) sont prélevés dans le réacteur (1'). Selon l'invention, l'amenée de la biomasse (3) et/ou le prélèvement des produits de la réaction (13, 15, 29, 29a, 29b, 29c, 29d,..., 29n) dans le réacteur (1') sont effectués pendant un déroulement en continu de la réaction. L'invention concerne par ailleurs un réacteur (1') servant à la mise en œuvre dudit procédé.
PCT/EP2012/051824 2011-02-18 2012-02-03 Procédé et réacteur de carbonisation hydrothermale de la biomasse WO2012110325A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102011004398.5 2011-02-18
DE201110004398 DE102011004398A1 (de) 2011-02-18 2011-02-18 Verfahren und Reaktor zur hydrothermalen Karbonisierung von Biomasse

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Publication Number Publication Date
WO2012110325A1 true WO2012110325A1 (fr) 2012-08-23

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WO (1) WO2012110325A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013079060A1 (fr) * 2011-12-02 2013-06-06 Thomas Reichhart Procédé et dispositif de carbonisation hydrothermale de biomasse

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012002098A1 (de) * 2012-02-06 2013-08-08 Eurofoam Deutschland Gmbh Hydrothermale Karbonisierung von Kunststoffmaterial
DE102013013085B3 (de) * 2013-08-07 2015-02-05 Eurofoam Deutschland Gmbh Schaumstoffe Partikel eines kohleähnlichen Feststoffs, Verwendungen und Herstellungsverfahren
DE102013018452B4 (de) 2013-11-02 2020-09-10 Vereinigung zur Förderung des Instituts für Kunststoffverarbeitung in Industrie und Handwerk an der Rhein.-Westf. Technischen Hochschule Aachen e.V. Verfahren zur Herstellung eines aus mindestens einer Kunststoffkomponente und mindestens einer Metallkomponente bestehenden Verbundbauteils
SE540135C2 (en) 2016-10-05 2018-04-10 C Green Tech Ab Method for hydrothermal carbonization of sludge in chemical pulp mills
CN109439379B (zh) * 2018-09-30 2023-10-24 昆明理工大学 一种生物燃料的制备系统

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EP1970431A1 (fr) * 2007-03-13 2008-09-17 Loritus GmbH Dispositif et procédé de carbonisation hydrothermale de biomasses
WO2010006881A1 (fr) * 2008-06-23 2010-01-21 Csl Carbon Solutions Ltd. Procédé de préparation d’un matériau hybride hydrothermal à partir d’une biomasse, et matériau hybride hydrothermal pouvant être obtenu par le procédé
EP2166061A1 (fr) * 2008-09-18 2010-03-24 Artes Biotechnology GmbH Dispositif et procédé destinés au traitement de biomasse
US20100162619A1 (en) * 2006-12-28 2010-07-01 Dominik Peus Material and/or fuel produced from biomass

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DE102007022840A1 (de) * 2007-05-11 2008-12-24 Suncoal Industries Gmbh Verfahren zur Kühlung und Vorwärmung einer Anlage zur hydrothermalen Carbonisierung von Biomasse
DE102008004732A1 (de) * 2008-01-16 2009-07-23 Lucia Viviane Sanders Hydrothermale Karbonisierung von Biomasse
DE202008012419U1 (de) * 2008-09-18 2008-11-20 Agrokraft Gmbh Vorrichtung zur Behandlung von Biomasse
DE102009007302C5 (de) * 2009-02-03 2019-04-25 Grebo License Gmbh & Co. Kg Verfahren und Vorrichtung zur hydrothermalen Karbonisierung von Biomasse
DE102009015257B4 (de) * 2009-04-01 2013-03-14 Suncoal Industries Gmbh Verfahren zur hydrothermalen Karbonisierung nachwachsender Rohstoffe und organischer Reststoffe

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100162619A1 (en) * 2006-12-28 2010-07-01 Dominik Peus Material and/or fuel produced from biomass
EP1970431A1 (fr) * 2007-03-13 2008-09-17 Loritus GmbH Dispositif et procédé de carbonisation hydrothermale de biomasses
WO2010006881A1 (fr) * 2008-06-23 2010-01-21 Csl Carbon Solutions Ltd. Procédé de préparation d’un matériau hybride hydrothermal à partir d’une biomasse, et matériau hybride hydrothermal pouvant être obtenu par le procédé
EP2166061A1 (fr) * 2008-09-18 2010-03-24 Artes Biotechnology GmbH Dispositif et procédé destinés au traitement de biomasse

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013079060A1 (fr) * 2011-12-02 2013-06-06 Thomas Reichhart Procédé et dispositif de carbonisation hydrothermale de biomasse

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