US20130199920A1 - Device and method for the thermochemical harmonising and gasification of wet biomass - Google Patents

Device and method for the thermochemical harmonising and gasification of wet biomass Download PDF

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US20130199920A1
US20130199920A1 US13/878,765 US201113878765A US2013199920A1 US 20130199920 A1 US20130199920 A1 US 20130199920A1 US 201113878765 A US201113878765 A US 201113878765A US 2013199920 A1 US2013199920 A1 US 2013199920A1
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reactor
carbonization
gasification
vessel
biomass
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Elhan Demir
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ZBB GmbH
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B39/00—Cooling or quenching coke
    • C10B39/04—Wet quenching
    • C10B39/08—Coke-quenching towers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/094—Char
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1693—Integration of gasification processes with another plant or parts within the plant with storage facilities for intermediate, feed and/or product
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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

Definitions

  • the invention relates to a device for the thermochemical carbonization and gasification of wet, especially water-containing and/or dry, biomass for producing an energy carrier and/or raw-material carrier by means of a heatable carbonization reactor having a closable inlet, in which the biomass is converted into a solid, pourable or gaseous energy carrier and/or raw-material carrier and is discharged via a closable outlet to a coolable vessel connected to the carbonization reactor for interim storage of the energy carrier and/or raw-material carrier, which is connected to a downstream gasification reactor, in which gas and waste substances, such as ash, are separated from the biomass.
  • Biomass gasification is generally known. This is understood as a process in which biomass is converted into a product gas or combustible gas by means of a gasifying or oxidizing agent (generally air, oxygen, carbon dioxide or steam) by partial combustion.
  • a gasifying or oxidizing agent generally air, oxygen, carbon dioxide or steam
  • the biomass that is in the form of solid fuel can be converted into a gaseous secondary fuel, which can be used more efficiently in various usage options, e.g. production of electricity or as fuel and propellant (combustible gas) or for use as synthesis gas for chemical synthesis.
  • Analogous processes also exist for other solid fuels, especially for the gasification of coal (coal gasification).
  • the gasification of biomass starts after drying at temperatures of approx. 150° C., with steam and oxygen being evolved first. At higher temperatures, the solid constituents of the biomass are burnt. This gas ignites as soon as secondary air is supplied; the flash point is from 230 to 280° C.
  • Industrial biomass gasification is partial combustion by means of a gasifying or oxidizing agent (generally air, oxygen, carbon dioxide or steam) without ignition at temperatures from 700 to 900° C., in which it is not oxidized to carbon dioxide (CO 2 ), as in combustion, but essentially to carbon monoxide (CO). Further components of the resultant gas are hydrogen (H 2 ), carbon dioxide (CO 2 ), methane (CH 4 ), steam (H 2 O) and a number of trace gases and impurities, depending on the biomass used. A solid residue is left (ash and coke); moreover, some fractions of the product gas may condense out as the temperature is lowered (tar and water).
  • a gasifying or oxidizing agent generally air, oxygen, carbon dioxide or steam
  • the combustible product gas can be oxidized further in a downstream process by combustion (combustible gas) or a chemical synthesis (synthesis gas) with release of energy (exothermic process). If the gasification takes place with air, the resultant product gas diluted with nitrogen is often also called lean gas (LCV, low calorific value gas).
  • combustion combustion
  • synthesis gas chemical synthesis
  • the resultant product gas diluted with nitrogen is often also called lean gas (LCV, low calorific value gas).
  • Hydrothermal carbonization (for instance: “aqueous carbonization at elevated temperature”) is a chemical process for simple and highly efficient production of lignite, synthesis gas, liquid petroleum precursors and humus from biomass with release of energy. In a few hours, the process technically duplicates the formation of lignite (“coalification”) that occurs in nature in 50 000 to 50 million years.
  • biomass especially plant material, (for simplicity represented as sugar, with the formula C 6 H 12 O 6 , in the following reaction equation) is heated to 180° C. together with water in an isochoric process in a pressure vessel.
  • the pressure may increase to 2 MPa.
  • oxonium ions are also formed, which lower the pH to pH 5 or lower.
  • the carbons pass into an aqueous phase and so are lost. This energy is no longer available for the working process.
  • This step can be accelerated by adding a small amount of citric acid. It must be borne in mind that at low values of pH, more carbon passes into the aqueous phase.
  • the reaction taking place is exothermic, i.e. energy is released.
  • the carbon of the educts has been converted completely: 90 to 99% of the carbon is in the form of solid phase as an aqueous sludge of porous lignite beads (C 6 H 2 O) with pore sizes between 8 and 20 nm; the remaining 1 to 10% of the carbon is either dissolved in the aqueous phase or has been converted to carbon dioxide.
  • the reaction equation for the formation of lignite is:
  • the reaction can be terminated in several stages with incomplete water cleavage, obtaining different intermediates. With termination after a few minutes there is formation of liquid intermediates, lipophilic substances, but their manipulation is very difficult on account of their high reactivity. Next, these substances polymerize and peat-like structures form, which after approx. 8 hours are available as intermediates.
  • reaction could be catalyzed with certain metal particles, but these would very quickly add onto the products and lose their function.
  • the artificially produced humus could be utilized for the revegetation of eroded areas. Through this intensified plant growth, additional carbon dioxide could be bound from the atmosphere, so that the final effect would be achievement of a carbon efficiency above 1 or a negative CO 2 balance.
  • the resultant coal slurry could be used for combustion or for operating novel types of fuel cells with an efficiency of 60%, which are currently under investigation at Harvard University.
  • the carbon/water mixture would first have to be heated strongly, so that so-called synthesis gas, a gas mixture of carbon monoxide and hydrogen, is formed:
  • liquid intermediates that form during incomplete reaction of the biomass could be used for producing fuels and plastics.
  • the resultant coal slurry could be briquetted and marketed as an environment-friendly—because it is carbon dioxide-neutral—“natural coal”, which, in comparison with the starting biomass, it should be possible by means of separation/filtration/compaction to dry with lower energy consumption and owing to its higher energy content per volume/mass would incur lower transport costs and would require less storage area.
  • the problem to be solved by the invention is to obtain more or less all the carbon and gases from the biomass and to produce these simply and economically.
  • reaction gas is recycled to the gasification reactor.
  • the method according to the invention preferably uses water-containing biomass, which mainly arises as municipal waste and in many cases must be disposed of at great expense. In this method it is, however, also possible to use other biomass, which does not have to be disposed of as residue.
  • At least two reactors are used for implementing the method. These are on the one hand the carbonization reactor and on the other hand the gasification reactor.
  • the energy required for evaporation is provided by utilizing heat that is released during cooling of the reactor gas produced.
  • reactor gas produced by the method according to the invention is almost completely free from tar or tar-forming constituents. This is in particular also achieved because the manner in which the process is managed means that the volatile, incombustible fractions from the biomass can be lowered from the existing 80% to approx. 30%, cf. Tables 1 and 2. The values for an installation of the prior art are given in Table 1 and for the equipment according to the invention in Table 2.
  • the reactor gas is cleaned by dust separation to remove solid particles, e.g. fine dust, and can then be utilized for producing power and heat.
  • the plant can be employed on a small industrial scale using gas-engine generator sets with heat utilization for supplying limited local areas of settlements with power and heat and in parallel for the disposal of suitable municipal wastes.
  • the problem of contamination of the gases and of tar formation is also solved in that there is almost complete internal disposal of critical reaction products in gaseous and vapor form through combustion in the gasification reactor.
  • hydrothermal carbonization is that the usable plant biomass is not restricted to plants with low moisture contents and the energy obtainable without carbon dioxide emissions is not reduced by the drying steps required or if necessary is directly usable for drying the end products.
  • the usable plant biomass is not restricted to plants with low moisture contents and the energy obtainable without carbon dioxide emissions is not reduced by the drying steps required or if necessary is directly usable for drying the end products.
  • even previously barely usable plant material such as clippings and prunings from gardens and from green areas in towns can be used for energy production, at the same time with a saving of carbon dioxide, which otherwise would be formed—together with the even more climate-damaging methane—during bacterial transformation of the biomass.
  • the operation of the complete plant is also energy-saving because almost all the thermal energy released is recycled to the working process.
  • the moisture-containing biomass received in the carbonization reactor is evaporated at pressures between 5 and 30 bar, preferably at pressures between 15 and 25 bar, especially at pressures of about 20 bar and at temperatures between 200° and 1200° C., preferably between 400° and 800° C., and reaction gas is formed, which is supplied directly or indirectly to the gasification reactor via a line.
  • the gasification reactor operates in a temperature range between 1200° and 1800° C., preferably between 1000° and 1400° C., and during the working process releases thermal energy via a line connecting the gasification reactor and the carbonization reactor.
  • a cyclone separator and/or gas scrubber is connected via a line to the gasification reactor, wherein a heat exchanger can be provided between the cyclone separator and/or gas scrubber, which lowers gas to the working temperature of the heat exchanger between 40° C. and 80° C. or between 50° C. and 60° C. and recycles the resultant abstracted energy to a heating system and/or to the working process of the plant.
  • the thermal energy released from the heat exchanger is supplied via a line to a consumer, such as a heating system.
  • the harmful substances or impurities released in the carbonization reactor and/or in the second vessel or buffer tank are destroyed or at least partially destroyed by means of a thermal device or are led away.
  • thermochemical carbonization and gasification device or the first vessel of wet, especially water-containing and/or dry, biomass is connected via a closable connection to a second vessel or buffer tank;
  • the first vessel and/or the second vessel or buffer tank are in each case connected via a line to a gas storage tank, especially reaction gas storage tank;
  • reaction gas storage tank is connected via the line to the gasification reactor;
  • the gasification reactor is connected directly or indirectly to a cleaning device, such as a cyclone separator and/or gas scrubber;
  • the thermal energy obtained or energy released in the gasification reactor is supplied via at least one line for process control of the thermochemical carbonization and gasification device or to the first vessel.
  • the gasification reactor is connected via a line to a processing device for treatment and/or further processing of the coal obtained in the gasification reactor.
  • the second vessel and/or the gasification reactor is connected via the line to the processing device for treatment or further processing of the coal obtained in the vessel and/or in the gasification reactor and a spun-bonded fabric or a ribbon fabric is used as carrying layer.
  • saturated steam is obtained in the gasification reactor, which is connected via a line conveying saturated steam to a consumer or to a heating system and/or a steam piston engine.
  • the gasification reactor is connected via at least one line to a consumer or at least to a gas compressor and/or gas engine.
  • the gasification reactor and/or the second vessel can be cooled by means of a cooling device, or in each case is surrounded by a cooling jacket and the cooling device is fed with cooling water, wherein at least also cooling water from the cooling jacket of the second vessel is supplied via a line to the gasification reactor.
  • the method is characterized by the following method steps:
  • the biomass is converted in a carbonization reactor by means of external thermal energy and further thermal energy, which is supplied from the plant to the carbonization reactor, into a solid, pourable or gaseous energy carrier and/or raw-material carrier;
  • reaction gas obtained or present in the first and second vessel is supplied directly or indirectly to the gasification reactor;
  • thermochemical carbonization and gasification of wet, especially water-containing and/or dry, biomass is recycled to the processing process, especially to the vessel;
  • the released energy produced in the gasification reactor or the saturated steam is supplied to one or more consumers, such as a heating system, and/or to a steam piston engine.
  • reaction gas produced in the complete plant or in the first vessel is supplied directly or indirectly to a cyclone separator and/or to a gas scrubber, then to a dehumidifier, or directly or indirectly via a compressor to the consumer.
  • control valves are provided, which can be turned off or on manually or by a drive device, wherein the drive devices can be controlled via a computer in relation to the working process.
  • FIG. 1 the flowsheet for a device for thermochemical carbonization and gasification of wet, especially water-containing and/or dry, biomass for producing an energy carrier and/or raw-material carrier by means of a heatable carbonization reactor that has a closable inlet, in which the biomass is converted into a solid, pourable or gaseous energy carrier and/or raw-material carrier;
  • FIG. 2 a general view of a device for thermochemical carbonization and gasification of wet, especially water-containing and/or dry, biomass for producing an energy carrier and/or raw-material carrier;
  • FIG. 3 a partial view of the device according to FIG. 1 ;
  • FIG. 4 a partial view of the gasification reactor with a gasifier head, a gasifier middle part and a gasifier bottom.
  • FIG. 1 shows a carbonization reactor or first vessel 1 for thermochemical carbonization and gasification of wet, especially water-containing and/or dry, biomass for producing an energy carrier and/or raw-material carrier.
  • the carbonization reactor or first vessel 1 is supplied with biomass via a receiving tank 2 , which is provided with an inlet valve or flat slide valve 13 and a flat slide valve or outlet valve 15 .
  • a stirrer 5 is provided, in which the biomass is mixed, which consists of a wet, especially water-containing and/or dry, biomass. This can include, among other things, wastes, such as foodstuff residues, biological wastes, and wood.
  • the stirrer 5 can be operated manually or by means of a motor 3 .
  • first wood or charcoal is put in a gasification reactor 16 and then the plant is started up.
  • the reaction gas obtained in the gasification reactor 16 is supplied via a line to a heating element 4 , which surrounds the carbonization reactor or first vessel 1 .
  • the carbonization is started.
  • the gas received in the heating element 4 is constantly cooled through introduction of biomass. Energy is saved as a result of this working process. The energy loss that arises is supplied to the plant with external energy.
  • the carbonization reactor or first vessel 1 is connected operatively to a heating element, in particular is surrounded by a heating jacket 4 .
  • the carbonization reactor 1 is supplied at least with external thermal energy 60 and in an advantageous, energy-saving manner with further thermal energy at least from the complete plant, especially from a gasification reactor 16 , so that in this way the plant can be operated very economically.
  • the biomass can be supplied continuously or batchwise to the vessel 1 .
  • a blow-off valve 7 for controlling the pressure of vessel is provided in the upper part of vessel 1 . If the biomass is supplied batchwise to vessel 1 , then vessel is filled with cold or also warmed biomass and is heated by the heating element, so that the water present in the biomass evaporates.
  • the steam is supplied to a reaction storage tank 21 , so that the energy, which is also made available to the gasification reactor 16 , can be fully utilized. With further heat supply above approx. 180° C., the chemical reaction starts and largely coal and gaseous reaction products are produced from the biomass.
  • the reaction gas led away from vessel 1 has a temperature of at least 300-400° C. This is led at least partially via line 28 into the reaction gas storage tank 21 and from there into the gasification reactor 16 . In line 28 there is a nonreturn valve 80 , so that excess pressure from the reaction gas storage tank 21 cannot escape to vessel 1 .
  • the gas is cooled by the cooling device 49 , which is connected via a line 51 and 30 to the vessel 9 , to a temperature of approx. 80°.
  • a pressure of approx. 2 to 5 bar prevails in vessel 9 and in the reaction gas storage tank 21 .
  • the cooling water is conveyed from the reaction gas storage tank 21 via a line 78 to the cooling jacket 52 of the gasification reactor 16 . As a result, more saturated steam can be produced. Via line 78 , the reaction gas storage tank 21 for the gasification reactor 16 can be emptied completely.
  • vessel 16 various measuring points 81 are provided, with the aid of which the temperature in vessel 16 can be controlled.
  • the gas storage tank 21 has a regulating function and serves for receiving the reaction gases from vessels 1 and 9 .
  • the reaction gas from the reaction gas storage tank 21 is burnt with the coal in the gasification reactor 16 .
  • the chemical reaction begins in the biomass and in addition to the biocoal there is also formation of gas, mainly CO 2 and steam.
  • This gas-steam mixture is called reaction exhaust gas.
  • the total pressure inside the reactor is found from the sum of the boiling pressure of steam and the partial pressure of the inert gas fraction in vessel 1 .
  • the reaction is associated with generation of heat, i.e. an exothermic reaction takes place in the vessel.
  • the carbonization reactor or first vessel 1 has the pressure-regulated or controlled valve 7 . After completion of the reaction, the carbonization reactor or first vessel 1 is relieved from pressure by fully opening valve 7 , until it can be opened safely and the biocoal can be removed.
  • the biomass is supplied to the carbonization reactor or first vessel 1 in small amounts and in short time intervals via a pressurized air lock or a receiving tank 9 from above.
  • a pressurized air lock or a receiving tank 9 In the carbonization reactor 1 there is always high pressure and high temperature of about 16 bar and 200° C.
  • the biomass supplied is heated in the carbonization reactor and the water it contains evaporates at least partially, or even completely, depending on the process time.
  • the reacting biomass passes through the reactor from top to bottom, with continuous stirring.
  • coal is removed from a second vessel or buffer tank 9 , also called a pressurized air lock.
  • reaction exhaust gas is released continually by the pressure control valve 7 from the carbonization reactor.
  • the pressurized air lock 9 can also be in the form of a buffer tank.
  • vessel 9 can be equipped with a stirrer, to ensure better penetration of the biocoal with moisture.
  • the plant can also be operated cyclically or with varying pressure, with a pressure of approx. 20 bar and a temperature of 200° C. in the carbonization reactor 1 .
  • the biocoal present in the second vessel or buffer tank 9 is cooled.
  • the vessel or buffer tank 9 has a cooling jacket 51 .
  • the pressure in the buffer tank 9 is also controlled by a pressure-controlled valve 12 , depending on how the process is operated.
  • the moisture-containing biomass received in the carbonization reactor 1 can evaporate at pressures between 5 and 30 bar, preferably at pressures between 15 and 25 bar, especially at pressures of about 20 bar and at temperatures between 200° and 1200° C., preferably between 400° and 800° C., and reaction gas can be formed, which is supplied directly or indirectly to the gasification reactor 16 via a line 30 .
  • the gasification reactor 16 operates at atmospheric pressure. It is subdivided into a gasifier head 61 , a gasifier middle part 62 and a gasifier bottom 63 .
  • the biocoal received in vessel 9 is fed via a feed hole 64 into the gasifier head 61 . There it is heated by the heat supplied from the gasifier middle part 62 to a temperature of up to approx. 900° C., at which the further gasification of the coal or biocoal begins.
  • the biocoal reaches the middle part 62 of the gasification reactor 16 .
  • gasification takes place at temperatures above 900° C.
  • the reaction gas that is released from the biocoal reaches temperatures of up to 1800° C.
  • the gasification reactor 16 consists of an outer casing 66 , in which a gasifier part 67 is housed in a funnel-shaped part, which has a larger cross section in the upper region than in the middle region.
  • the bottom of the gasification reactor 63 gets wider toward its discharge end.
  • the discharge end consists of several outlets 68 provided in the gasification reactor bottom 63 for discharge of the reactor gas and the ash.
  • the reactor gas is led via the outlets 68 in a perforated, partially cylindrically or conically expanded, internal wall 69 of the gasification reactor bottom 63 into an annular gap 70 that is formed between an external wall 71 and the internal wall 69 of the gasification reactor bottom 63 .
  • the gasification reactor 16 is also connected directly or indirectly to a cleaning device, such as a cyclone separator 18 and/or gas scrubber 20 . From there, the gas is conveyed to a gas compressor 44 and/or to a gas engine 48 .
  • the gasification reactor 16 is also connected via line to the reaction gas storage tank 21 ( FIG. 1 ).
  • the gasification reactor 16 has maintenance openings 82 , which can be opened if necessary.
  • outlets 72 distributed round the circumference, through which the reactor gas is withdrawn from the gasification reactor 16 .
  • Lines 73 connected thereto open into one or more dust separators, which are for example in the form of cyclone separators 18 and from which the reactor gas is supplied for further use or is supplied to the consumers, such as the gas engine 48 or gas compressor 44 .
  • the ash is discharged at the lower end of the gasification reactor bottom 63 via an outlet 65 and is transported from there by a conveyor to a disposal tank.
  • one or more gas lances or thermally connected melting units 74 are provided, so that reaction exhaust gas 75 from the carbonization reactor 1 and optionally also from the second vessel or buffer tank or the pressurized air lock 9 can be injected into the gasification zone of the gasification reactor 16 .
  • reaction exhaust gas 75 from the carbonization reactor 1 and optionally also from the second vessel or buffer tank or the pressurized air lock 9 can be injected into the gasification zone of the gasification reactor 16 .
  • the gasification reactor 16 ( FIGS. 1 and 4 ) and/or the second vessel 9 are cooled by means of a cooling device 49 and are in each case surrounded by a cooling jacket 51 , 52 .
  • the cooling device 49 is fed with cooling water, wherein at least also cooling water from the cooling jacket 51 of the second vessel 9 can be supplied via a line 54 to the gasification reactor 16 .
  • the heat taken up by the coolant can be used for evaporation of the cooling water and for superheating the high-pressure steam 76 thus produced.
  • the gasification reactor 16 can be operated continuously.
  • the biomass is supplied in short time intervals or continuously.
  • the reactor gas and the ash are discharged continuously as volume or mass flows from the gasification reactor 16 .
  • the reactors 1 and 16 described are operated roughly simultaneously.
  • the carbonization reactor 1 By arranging the carbonization reactor 1 , the buffer tank 9 and the gasification reactor 16 according to FIG. 4 as an operational unit, a space-saving arrangement is achieved.
  • the biomass feed is located above the complete device, consisting of 1 , 9 , 16 .
  • the biomass is received via the entry pressurized air lock in the receiving tank 2 and is supplied to the gasification reactor 16 . It passes through this from top to bottom and on completion of carbonization is discharged into the buffer tank 9 .
  • the buffer tank 9 In continuous operation of the carbonization reactor 1 , the buffer tank 9 , which receives biocoal from the carbonization reactor 1 , is operated intermittently.
  • the moisture-containing biomass received in the carbonization reactor 1 evaporates at pressures between 5 and 30 bar, preferably at pressures between 15 and 25 bar, especially at pressures of about 20 bar and at temperatures between 200° and 1200° C., preferably between 400° and 800° C.
  • Reaction gas is also formed, which is supplied directly or indirectly to the gasification reactor 16 via line 30 .
  • FIG. 4 Another possibility for construction of the complete device, consisting of vessels 1 , 9 , 16 , is shown in FIG. 4 . This is suitable when a vertical arrangement is not possible for reasons of space.
  • the biocoal leaving the buffer tank 9 is transported by means of mechanical conveying devices, such as a conveyor belt or worm conveyor 77 , into the filling hopper of the adjacent gasification reactor 16 , feeding the latter continuously.
  • mechanical conveying devices such as a conveyor belt or worm conveyor 77
  • FIG. 3 A flow chart of the complete plant is shown in FIG. 3 .
  • the gasification reactor 16 is connected via a line 34 to a further processing device 36 for treatment and/or further processing of the coal obtained in the gasification reactor 16 .
  • the saturated steam that is formed in the gasification reactor 1 is connected via the saturated steam line 38 to a consumer or to a heating system and/or a steam piston engine 42 .
  • reaction gas produced in the complete plant or in the first vessel 1 is supplied directly or indirectly to the cyclone separator 18 and/or gas scrubber 20 and then to a dehumidifier 56 or directly or indirectly to a compressor 44 or to the consumer 48 .
  • control valves can be provided, which can be turned on or off manually or by a drive device, wherein the drive devices are controlled via a computer in relation to the working process.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
US13/878,765 2011-02-14 2011-02-14 Device and method for the thermochemical harmonising and gasification of wet biomass Abandoned US20130199920A1 (en)

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US20150059245A1 (en) * 2013-09-05 2015-03-05 Ag Energy Solutions, Inc. Apparatuses, systems, mobile gasification systems, and methods for gasifying residual biomass
US9631151B2 (en) 2014-09-04 2017-04-25 Ag Energy Solutions, Inc. Apparatuses, systems, tar crackers, and methods for gasifying having at least two modes of operation
US20180119040A1 (en) * 2015-04-22 2018-05-03 North-West University Production of a carbonaceous feedstock material from a waste carbon source
EP3492558A4 (en) * 2016-07-29 2019-06-05 Tongji University METHOD AND SYSTEM FOR THE PRODUCTION OF FUEL GAS USING ORGANIC WASTE WITH HIGH WATER CONTENT
US11015136B2 (en) * 2016-03-11 2021-05-25 King Abdullah University Of Science And Technology Supercritical water gasification with decoupled pressure and heat transfer modules
EP3950606A1 (en) * 2020-08-07 2022-02-09 HBI S.r.l. Biomass treatment process and plant
US11827859B1 (en) 2022-05-03 2023-11-28 NuPhY, Inc. Biomass gasifier system with rotating distribution manifold

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CN111378464B (zh) * 2020-03-25 2022-02-25 重庆交通大学 一种水热碳化技术处理餐厨垃圾的家用小型原位处理设备及全封闭回收系统

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4123406C2 (de) * 1991-07-15 1995-02-02 Engineering Der Voest Alpine I Verfahren zum Vergasen von minderwertigen festen Brennstoffen in einem schachtförmigen Vergasungsreaktor
DE4404673C2 (de) * 1994-02-15 1995-11-23 Entec Recycling Und Industriea Verfahren zur Erzeugung von Brenngas
CA2501841C (en) * 2004-03-23 2012-07-10 Central Research Institute Of Electric Power Industry Carbonization and gasification of biomass and power generation system
CN2698791Y (zh) * 2004-05-26 2005-05-11 河南省焦作市秸秆燃气有限公司 生物质干馏炭化气化装置
CN1699512A (zh) * 2005-07-04 2005-11-23 刘伟奇 生物质洁净燃气发生装置及其洁净燃气的制备方法
CN100575455C (zh) * 2006-09-21 2009-12-30 武汉凯迪科技发展研究院有限公司 生物质深度脱水炭化连续处理工艺及其设备
CN1931959B (zh) * 2006-09-28 2010-10-20 武汉凯迪工程技术研究总院有限公司 利用生物质制造合成气的复合循环式高温气化工艺方法
DE102007005799B4 (de) * 2006-10-18 2018-01-25 Heinz-Jürgen Mühlen Verfahren zur Erzeugung eines wasserstoffreichen Produktgases
RU2341552C1 (ru) * 2007-06-13 2008-12-20 Общество с ограниченной ответственностью "Углеводород" Способ получения синтез-газа
JP5397878B2 (ja) * 2008-07-04 2014-01-22 一般財団法人電力中央研究所 バイオマス燃料を用いたガス化設備及びガス化発電設備
DE102008047201B4 (de) * 2008-09-15 2011-10-06 Semiha Pektas-Cehreli Verfahren und Vorrichtung zur Produktion von Synthesegas und zum Betreiben eines Verbrennungsmotors damit
CN101418239B (zh) * 2008-12-01 2011-12-21 武汉凯迪工程技术研究总院有限公司 利用生物质制造合成气的高温气化工艺方法及系统

Cited By (11)

* Cited by examiner, † Cited by third party
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US20150059245A1 (en) * 2013-09-05 2015-03-05 Ag Energy Solutions, Inc. Apparatuses, systems, mobile gasification systems, and methods for gasifying residual biomass
US9567539B2 (en) * 2013-09-05 2017-02-14 Ag Energy Solutions, Inc. Apparatuses, systems, mobile gasification systems, and methods for gasifying residual biomass
US9631151B2 (en) 2014-09-04 2017-04-25 Ag Energy Solutions, Inc. Apparatuses, systems, tar crackers, and methods for gasifying having at least two modes of operation
US20180119040A1 (en) * 2015-04-22 2018-05-03 North-West University Production of a carbonaceous feedstock material from a waste carbon source
AU2016252354B2 (en) * 2015-04-22 2019-08-01 North-West University Production of a carbonaceous feedstock material from a waste carbon source
US10711214B2 (en) * 2015-04-22 2020-07-14 North-West University Production of a carbonaceous feedstock material from a waste carbon source
US11015136B2 (en) * 2016-03-11 2021-05-25 King Abdullah University Of Science And Technology Supercritical water gasification with decoupled pressure and heat transfer modules
EP3492558A4 (en) * 2016-07-29 2019-06-05 Tongji University METHOD AND SYSTEM FOR THE PRODUCTION OF FUEL GAS USING ORGANIC WASTE WITH HIGH WATER CONTENT
US10611657B2 (en) 2016-07-29 2020-04-07 Tongji University Method and system for preparing fuel gas by utilizing organic waste with high water content
EP3950606A1 (en) * 2020-08-07 2022-02-09 HBI S.r.l. Biomass treatment process and plant
US11827859B1 (en) 2022-05-03 2023-11-28 NuPhY, Inc. Biomass gasifier system with rotating distribution manifold

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DE112011104882A5 (de) 2013-11-28
DK2507346T3 (en) 2016-01-11
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CA2800606A1 (en) 2012-08-23
JP2014505149A (ja) 2014-02-27
RU2562112C2 (ru) 2015-09-10
PL2507346T3 (pl) 2016-03-31
JP5938788B2 (ja) 2016-06-22
RU2012151909A (ru) 2015-01-10
CN102959056B (zh) 2014-11-19
ES2558318T3 (es) 2016-02-03
CA2800606C (en) 2018-01-02
EP2507346A1 (de) 2012-10-10
WO2012110012A1 (de) 2012-08-23
PL2507346T4 (pl) 2016-04-29

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