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US20120111715A1 - Method and System for Utilizing Biomass and Block-Type Thermal Power Plant - Google Patents

Method and System for Utilizing Biomass and Block-Type Thermal Power Plant Download PDF

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Publication number
US20120111715A1
US20120111715A1 US13/256,111 US201013256111A US2012111715A1 US 20120111715 A1 US20120111715 A1 US 20120111715A1 US 201013256111 A US201013256111 A US 201013256111A US 2012111715 A1 US2012111715 A1 US 2012111715A1
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United States
Prior art keywords
dryer
heat
stage
pyrolysis
transfer circuit
Prior art date
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Abandoned
Application number
US13/256,111
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English (en)
Inventor
Bernd Johannes Krois
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.)
Uniper Anlagenservice GmbH
Original Assignee
EOn Anlagenservice GmbH
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Filing date
Publication date
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Assigned to E.ON ANLAGENSERVICE GMBH reassignment E.ON ANLAGENSERVICE GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KROIS, BERND JOHANNES
Publication of US20120111715A1 publication Critical patent/US20120111715A1/en
Abandoned legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/001—Heating arrangements using waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/10—Heating arrangements using tubes or passages containing heated fluids, e.g. acting as radiative elements; Closed-loop systems
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/06—Sludge reduction, e.g. by lysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/10—Energy recovery
    • 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 good
    • F26B2200/18—Sludges, e.g. sewage, waste, industrial processes, cooling towers
    • 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
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • 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
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

Definitions

  • the invention relates to a method for utilising biogenic mass, in particular sewage sludge, in which the material to be utilised is first dried and then thermally decomposed in a pyrolysis reactor for the purpose of generating pyrolysis gas.
  • the invention further relates to a system for utilising biogenic mass.
  • biogenic mass includes “biomass” in accordance with the German Biomass Ordinance, that is to say vegetable residues, waste and by-products of vegetable and animal origin, biowaste, waste wood, etc. and also recycled process waste and domestic and industrial sewage sludges.
  • the incineration of sewage sludge in decentralised power plants also leads only to little success in terms of reduced process costs. Although the transport routes are generally shortened, the energy obtained from the incineration process is still too low compared to the energy to be consumed for the drying process. Furthermore, the incineration process has to be maintained using additional fuels, wherein it is approximately only these which account for an ultimately positive energy balance.
  • a further possibility of utilisation of sewage sludge lastly consists of fermentation in biogas systems.
  • a central drawback in this instance is that the yields of biogas are too low and therefore the efficiency of the method is also too low.
  • the object of the invention is to provide a method and a system for utilising biogenic mass, in particular sewage sludge, which method and system can be operated with high efficiency based on the energy content of the introduced biogenic mass in relation to the energy generated by the utilisation.
  • the object is achieved with a method for utilising biogenic mass, in particular sewage sludge, according to the preamble of claim 1 , in that the material is thermally dried in at least two dryer stages arranged in succession, wherein the waste heat of the dryer stage arranged downstream in the direction of transport of material is used as process heat for the dryer stage arranged upstream.
  • the specific advantage of the method according to the invention is that, owing to the use of the waste heat of the downstream dryer stage as useful heat in the upstream dryer stage, the energy to be provided for the necessary drying of the biogenic mass can thus be minimised overall, and therefore the energy obtained for example during a combustion of the pyrolysis gas obtained during the pyrolysis process is much greater than the energy to be applied for the drying of the biogenic mass, which was not previously possible in comparable methods of the prior art.
  • the applicant's calculations have demonstrated that an energy recovery from biogenic mass of approximately up to 80% is possible based on the energy content thereof.
  • a further advantage of the method according to the invention is that it can be operated in a fully decentralised manner, for example since the biogenic mass can be dried and pyrolysed in the vicinity of the location of its origin, that is to say in the case of sewage sludge in the vicinity of a sewage treatment plant, wherein the pyrolysis gas can optionally then be used in a fuel cell or in a heat engine connected to a generator, for example a gas turbine, a combustion engine or a Stirling engine to produce electricity.
  • a generator for example a gas turbine, a combustion engine or a Stirling engine to produce electricity.
  • useful heat can be obtained in addition to electricity, and therefore the method according to the invention is also significant in terms of the desired increased use of power-heat-cogeneration.
  • the at least two dryer stages preferably comprise at least one low-temperature dryer as an upstream dryer stage and at least one high-temperature dryer as a downstream dryer stage.
  • the waste heat of the high-temperature stage is thus made available to the low-temperature stage as process heat, and is utilised in the system, that is to say in the process inherent to the system.
  • dryer stages may be provided in addition to a low-temperature stage and a high-temperature stage, and therefore a dryer cascade formed of a plurality of dryer stages can also be formed, in which each next highest dryer stage arranged downstream in the direction of transport of the material to be dried makes its waste heat available as process heat to the upstream dryer stage or to the upstream dryer stages which is/are at a lower temperature.
  • the heat of the waste gases of the auxiliary burner firing the pyrolysis reactor is used as process heat in the upstream dryer stage and/or the downstream dryer stage.
  • the principle upon which the invention is based is thus extended to the effect that the waste heat of the pyrolysis reactor, which is also still at a much greater temperature level compared to a high-temperature dryer stage, is made available to one or more dryer stages as process heat.
  • the waste heat of a downstream process stage is thus made available as process heat to the upstream process stages of lower temperature.
  • the heat of the hot pyrolysis gas produced in the pyrolysis reactor can also be used as process heat in the upstream dryer stage and/or in the downstream dryer stage.
  • the high thermal energy content of the pyrolysis gas can thus be fed as process heat to the dryer stages arranged upstream of the pyrolysis reactor, the efficiency of the entire process thus being further increased.
  • the pyrolysis gas produced in the pyrolysis reactor is fed to an energy converter unit for conversion of the energy content of the pyrolysis gas into electricity.
  • a fuel cell which converts the chemical energy content of the pyrolysis gas directly into electricity can be considered an energy converter unit, as can a heat engine driving a generator, in particular a gas turbine, a combustion engine or a Stirling engine.
  • the heat of the waste gases of the heat engine can be used as process heat in the upstream dryer stage and/or in the downstream dryer stage.
  • each of the at least two dryer stages is supplied with process heat via its own heat transfer circuit, in particular a thermal oil circuit.
  • the waste heat can thus be conveyed to the downstream dryer stage, in particular in the form of exhaust vapours, that is to say in the form of a steam-air mixture, by a heat exchanger integrated into the heat transfer circuit of the upstream dryer stage so as to be used in accordance with the invention as process heat for the upstream dryer stage.
  • the waste heat of the waste gases thereof is used as process heat for the upstream dryer stage and/or the downstream dryer stage, this may take place in practice in that the waste gases of the heat engine are conveyed through a waste gas heat exchanger integrated into the heat transfer circuit of the respective dryer stage.
  • a waste gas heat exchanger integrated into the heat transfer circuit of the downstream dryer stage whereupon it is then conveyed through a heat exchanger integrated into the heat transfer circuit of the upstream dryer stage.
  • the exhaust vapours flowing off from a dryer stage may also supply, at least in part, the necessary process heat for this dryer stage itself, in that at least some of the exhaust vapours are first compressed with the addition of energy, heated and then condensed in a heat exchanger integrated into the heat transfer circuit of the respective dryer stage, wherein the condensation enthalpy is delivered to the heat transfer circuit and the heat transfer medium is heated.
  • the waste heat of the dryer stage is thus raised to a higher temperature level by compression in the manner of a heat pump and is then fed in the form of useful heat via a heat exchanger acting as a condenser back into the heat transfer circuit supplying the dryer stage with process heat.
  • some of the pyrolysis gas produced in the pyrolysis reactor is used as fuel for the burner of a boiler, in particular a thermal oil boiler, integrated into the heat transfer circuit of the upstream and/or downstream dryer stage.
  • the boiler is preferably arranged in the heat transfer circuit of the downstream dryer stage and the waste gases of the boiler burner are then guided through a heat exchanger integrated into the heat transfer circuit of the upstream dryer stage.
  • the energy content of the branched off pyrolysis gas is used in a particularly efficient manner for both of the at least two dryer stages.
  • the system can be operated basically independently of further fuels.
  • the pyrolysis coke produced during pyrolysis of the dried material may be fed to a gasifier and for the lean gas produced there by gasification to be fed as fuel to the auxiliary burner for the pyrolysis reactor.
  • the object mentioned at the outset is achieved with a system for utilising biogenic mass, in particular Of sewage sludge, according to the preamble of claim 17 , in that the dryer device comprises at least two dryer stages arranged in succession in the direction of transport of the material and coupled to one another in such a way that the waste heat of the dryer stage arranged downstream in the direction of transport of the material can be used as useful heat for the dryer stage arranged upstream.
  • FIG. 1 is a block diagram of a system for generating electricity from sewage sludge
  • FIG. 2 shows of a block diagram of the low-temperature dryer comprising a thermal oil circuit, according to a preferred embodiment
  • FIG. 3 shows a preferred embodiment of the pyrolysis reactor of the system from FIG. 1 ;
  • FIG. 4 is a flow chart illustrating a method for utilising sewage sludge.
  • the system illustrated schematically in the form of a block diagram in FIG. 1 for generating electricity from sewage sludge as biogenic mass comprises a dryer device 1 , through which the sewage sludge introduced into the system at a feed point 1 a is transported and dried.
  • the dryer device is divided into two dryer stages, that is to say a low-temperature dryer 3 and a high-temperature dryer 4 . Further dryer stages may be added (not shown in this case).
  • a pyrolysis reactor 2 is arranged behind the high-temperature dryer 4 in the process direction and is fired by an auxiliary burner 2 a.
  • pyrolysis gas normally consisting of nitrogen, carbon dioxide, hydrogen, carbon monoxide and higher carbon atoms
  • pyrolysis coke and ash which cannot be utilised further are produced.
  • the pyrolysis gas escapes from the pyrolysis reactor 2 via a line 25 and arrives in a heat engine, in this case a gas turbine 5 , which in turn is connected to a generator 5 a for generating electricity.
  • a heat engine in this case a gas turbine 5 , which in turn is connected to a generator 5 a for generating electricity.
  • a combustion engine, a Stirling engine or a fuel cell which converts the chemical energy of the pyrolysis gas directly into electricity may also be provided instead of a gas turbine.
  • the thermal oil circuits 30 , 40 can be coupled to one another (not shown in FIG. 1 ), which is advantageous in particular when starting up the system so as to achieve rapid drying of the sewage sludge until a steady operating state is reached.
  • a thermal oil boiler 41 for heating the thermal oil and a heat exchanger 42 are arranged in succession in the thermal oil circuit 40 of the high-temperature dryer 4 .
  • the thermal oil boiler 41 comprises an auxiliary burner 41 a, of which the fuel feed line 43 is connected to the pyrolysis gas line 25 .
  • the auxiliary burner 41 a is accordingly operated directly with the pyrolysis gas produced in the pyrolysis reactor 2 as fuel.
  • the thermal oil circulating in the thermal oil circuit 40 is additionally heated by the hot waste gases flowing off via a waste gas line 52 from the gas turbine 5 .
  • a total of five heat exchangers 31 to 35 are arranged in succession in the thermal oil circuit 30 of the low-temperature dryer 3 .
  • the waste gases of the burner 41 a of the thermal oil boiler 41 arranged in the thermal oil circuit 40 flow through the heat exchanger 31 .
  • the residual heat of the waste gases flowing out from the heat exchanger 31 escapes as lost heat.
  • the waste gases of the gas turbine 5 flow through the heat exchanger 32 once they have already passed through the heat exchanger 42 arranged in the thermal oil circuit 40 .
  • the connection of the heat exchanger 42 , 32 is merely indicated in FIG. 1 by the symbols C-C.
  • the residual heat of the waste gases of the gas turbine escapes, again as lost heat, after passing through the heat exchanger 32 , wherein the thermal oil circulating in the thermal oil circuit 30 is further heated.
  • the thermal oil of the thermal oil circuit 30 is further heated by the waste gases of the auxiliary burner 2 a of the pyrolysis reactor 2 .
  • these waste gases flow through the waste gas line 23 and into the heat exchanger 33 integrated into the line.
  • the line 44 through which the exhaust vapours exiting from the high-temperature dryer 4 flow is connected to the heat exchanger 34 of the thermal oil circuit 30 , in such a way that the exhaust vapours flow through the heat exchanger 34 and deliver some of their thermal energy to the thermal oil.
  • the heat exchanger 35 is arranged in the thermal oil circuit 30 of the low-temperature dryer 3 .
  • the hot pyrolysis gases exiting from the pyrolysis reactor 2 flow through said heat exchanger, wherein some of their heat is delivered to the thermal oil.
  • FIG. 2 shows a block diagram of a particularly preferred embodiment of the low-temperature dryer 3 .
  • a further heat exchanger 37 is integrated into the thermal oil circuit 30 of the low-temperature dryer 3 .
  • the heat exchangers 31 to 35 described above are not shown in FIG. 2 .
  • the exhaust vapours flowing out from the low-temperature dryer 3 are compressed in a compressor 36 in accordance with the arrangement of FIG. 2 , wherein they are raised to a higher temperature level and then flow as a compressed exhaust vapour flow through the line 38 into the heat exchanger 37 , which acts as a condensation heat exchanger.
  • the exhaust vapours are accordingly liquefied as they pass through the heat exchanger 37 , wherein the condensation heat is delivered to the thermal oil circulating in the thermal oil circuit 30 .
  • further process heat for the drying process in the low-temperature dryer 3 can be provided in a very efficient manner by the use of additional energy in the compressor.
  • FIG. 3 shows a block diagram of a particularly preferred embodiment of the pyrolysis reactor 2 of the system of FIG. 1 .
  • the components already known from the block diagram of FIG. 1 bear corresponding reference numerals.
  • the specific feature of the arrangement illustrated in FIG. 3 is that the pyrolysis coke produced during the pyrolysis process is recovered from the reactor via a line 24 and is fed to a gasifier stage 26 , where the pyrolysis coke is gasified in ways known per se from the prior art.
  • the lean gas produced is cleaned in a cleaning stage 27 and is then fed to the auxiliary burner 2 a of the pyrolysis reactor 2 as additional fuel.
  • the efficiency of the entire method is thus further increased since further pyrolysis products, in this instance the pyrolysis coke, are utilised as an energy source in the process.
  • the sewage sludge to be dried having a dry substance content of normally approximately 25% (the remaining 75% is formed by water) is fed into the system and transported into the low-temperature dryer 3 and pre-dried. Here, it is dried until it has a dry substance content after leaving the low-temperature dryer 3 of approximately 40%.
  • the low-temperature dryer 3 is supplied with the necessary process heat by the thermal oil circuit 30 .
  • the pre-dried material is then conveyed into the high-temperature dryer 4 and is dried until reaching the final degree of dryness.
  • the exhaust vapours produced in the high-temperature dryer 4 are conveyed via the line 44 into the heat exchanger 34 provided in the thermal oil circuit 30 of the low-temperature dryer 3 , where they deliver some of their heat to the thermal oil circulating in the thermal oil circuit 30 .
  • the waste heat of the dryer stage arranged downstream in the direction of transport of the material that is to say the waste heat of the high-temperature dryer 4 , is thus used as process heat for the dryer stage arranged upstream, i.e. the low-temperature dryer 3 .
  • the material dried to a dry substance content of approximately 85% is then fed into the pyrolysis reactor 2 , where the material is preferably thermally decomposed in a two-stage pyrolysis process in the absence of oxygen, as is known per se from the prior art.
  • the heat necessary for this is generated by the auxiliary burner 2 a.
  • the burner waste gas produced is fed via the line 23 to the heat exchanger 33 provided in the thermal oil circuit 30 of the low-temperature dryer 3 , and therefore the heat of the burner waste gases is also used as process heat in a dryer stage, in this case in the low-temperature dryer 3 .
  • the pyrolysis gas produced in the pyrolysis reactor 2 leaves the pyrolysis reactor 2 via the line 25 and first passes through a dust separator 21 , where any dusts still contained in the pyrolysis gas flow are separated. As can be seen in FIG. 1 , the pyrolysis gas then flows through the heat exchanger 35 so that the heat of the pyrolysis gas produced in the pyrolysis reactor 2 is again fed as process heat to this dryer stage.
  • the pyrolysis gas flow is branched off from the line 25 into the lines 22 , 43 .
  • the pyrolysis gas fed into the line 22 is used as fuel to fire the auxiliary burner 2 a of the pyrolysis reactor 2
  • the fraction fed into the line 43 is fed as fuel to the auxiliary burner 41 a of the thermal oil boiler 41 arranged in the thermal oil circuit 40 of the high-temperature dryer 4 .
  • the chemical energy contained in the pyrolysis gas produced in the pyrolysis reactor 2 is thus used in a particularly efficient manner to maintain the entire process.
  • the pyrolysis gas flowing through the line 25 is then fed into the gas turbine 5 , where it is combusted, wherein the gas turbine 5 drives a generator 5 a.
  • the waste gases of the gas turbine are fed through the line 52 to the heat exchanger 42 arranged in the thermal oil circuit 40 of the high-temperature dryer 4 and are then fed to the heat exchanger 32 arranged in the thermal oil circuit 30 of the low-temperature dryer 3 so that the heat contained in the waste gas of the gas turbine is again made available to the two dryer stages 3 , 4 as process heat.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • General Engineering & Computer Science (AREA)
  • Sustainable Development (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Thermal Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Treatment Of Sludge (AREA)
  • Processing Of Solid Wastes (AREA)
US13/256,111 2009-03-13 2010-01-29 Method and System for Utilizing Biomass and Block-Type Thermal Power Plant Abandoned US20120111715A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE200910012668 DE102009012668A1 (de) 2009-03-13 2009-03-13 Verfahren und Anlage zur Verwertung von Biomasse
DE102009012668.6 2009-03-13
PCT/EP2010/051063 WO2010102854A1 (de) 2009-03-13 2010-01-29 Verfahren und anlage zur verwertung von biomasse sowie blockheizkraftwerk

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US20120111715A1 true US20120111715A1 (en) 2012-05-10

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US (1) US20120111715A1 (pt)
EP (1) EP2406190B1 (pt)
JP (1) JP2012520166A (pt)
KR (1) KR20110137345A (pt)
CN (1) CN102348649A (pt)
BR (1) BRPI1009134A2 (pt)
CA (1) CA2755375A1 (pt)
DE (1) DE102009012668A1 (pt)
RU (1) RU2011141417A (pt)
WO (1) WO2010102854A1 (pt)

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WO2013182930A3 (en) * 2012-05-25 2014-03-13 Tm.E. S.P.A. Termomeccanica Ecologia Plant for the treatment of sludge
EP2774894A1 (en) * 2013-03-08 2014-09-10 Sociedad General de Aguas de Barcelona, S.A. Continuously operating method for the thermal hydrolysis of organic material and installation for implementing the method
US20150336832A1 (en) * 2014-05-21 2015-11-26 Leaderman & Associates Co., Ltd. Sludge processing equipment
KR20170072320A (ko) * 2014-10-24 2017-06-26 종잉 창지앙 인터내셔널 뉴 에너지 인베스트먼트 컴퍼니 리미티드 발전소 연도 가스로부터의 과열을 이용하여 바이오매스 연료를 건조하기 위한 방법 및 장치
WO2017212188A1 (fr) * 2016-06-09 2017-12-14 Haffner Energy Dispositif de sechage
FR3052544A1 (fr) * 2016-06-08 2017-12-15 Haffner Energy Dispositif de deshydratation
WO2018073344A1 (en) * 2016-10-20 2018-04-26 Hsl Energy Holding Aps Plant and process for production of hot water from humid air
US11215360B2 (en) * 2015-08-18 2022-01-04 Glock Ökoenergie Gmbh Method and device for drying wood chips
US11248824B2 (en) * 2017-10-31 2022-02-15 Jiangsu Tenesun Electrical Appliance Co., Ltd. Control system and control method for frostless, multivariable coupling, and heat pump-based hot blast stove
US20220146094A1 (en) * 2020-11-09 2022-05-12 Guangdong University Of Technology System for disposing high-moisture mixed waste composed of kitchen garbage and water-containing sludge

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CN102348649A (zh) 2012-02-08
DE102009012668A1 (de) 2010-09-16
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