EP3969545A1 - Procédé pour le recyclage d'au moins une matière de valeur contenue dans une biomasse - Google Patents

Procédé pour le recyclage d'au moins une matière de valeur contenue dans une biomasse

Info

Publication number
EP3969545A1
EP3969545A1 EP20718519.0A EP20718519A EP3969545A1 EP 3969545 A1 EP3969545 A1 EP 3969545A1 EP 20718519 A EP20718519 A EP 20718519A EP 3969545 A1 EP3969545 A1 EP 3969545A1
Authority
EP
European Patent Office
Prior art keywords
coke
pyrolysis
gasifier
gas
fed
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP20718519.0A
Other languages
German (de)
English (en)
Inventor
Bernd MICKISCH
Peter ILLECKER
Udo PROKSCH
Andreas Hackl
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.)
Next Generation Elements GmbH
Original Assignee
Next Generation Elements GmbH
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
Priority claimed from ATA50176/2019A external-priority patent/AT522257A1/de
Application filed by Next Generation Elements GmbH filed Critical Next Generation Elements GmbH
Publication of EP3969545A1 publication Critical patent/EP3969545A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • 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
    • C10J2300/0923—Sludge, e.g. from water treatment plant
    • 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
    • C10J2300/0943—Coke
    • 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
    • C10J2300/0969—Carbon dioxide
    • 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
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • 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
    • C10J2300/1815—Recycle loops, e.g. gas, solids, heating medium, water for carbon dioxide
    • 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
    • C10J2300/1861—Heat exchange between at least two process streams
    • 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
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1869—Heat exchange between at least two process streams with one stream being air, oxygen or ozone
    • 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
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1876—Heat exchange between at least two process streams with one stream being combustion gas
    • 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 thermo-chemi see treatment of biomass, in particular organic waste products, and the recovery of at least one valuable material contained in the biomass.
  • DE 10 2008 028 241 A1 describes a device for thermo-chemi see Elmwand development of biomass in a fuel gas.
  • the device consists of a screw reactor and another reactor.
  • the biomass is dried and pyrolysed with the exclusion of air, the pyrolysis coke produced in the process, the pyrolysis gas and water vapor being fed together to the further reactor, which is filled with the formation of a pyrolysis coke bed.
  • partial oxidation takes place through the sub-stoichiometric addition of a gasification agent, in particular air.
  • the long-chain tar molecules are at least partially split up.
  • the residues are withdrawn from the further reactor at the bottom by means of a withdrawal device.
  • a large number of interior extensions extending at least partially in the direction of gravity are provided.
  • the resulting fuel gas is fed to a gas filter and a gas cooler via its own outlet openings.
  • the cleaned fuel gas flowing out of the outlet of the gas cooler is then fed to a gas engine, for example.
  • the electrical energy generated in the gas engine can be fed into the supply network, whereby the heat generated can also be used to heat the aforementioned screw reactor.
  • the object of the present invention was to provide a method by means of which a user is able to treat a biomass in such a way that at least one valuable material contained therein can be recovered and thus a residue product is created, which in particular as Fertilizers can be used. Furthermore, the burning of biomass as a classic disposal route is also to be avoided. This object is achieved by a method according to the claims.
  • the method is used to see thermo-chemical treatment of biomass, in particular of organic waste products such as sewage sludge, slaughterhouse waste, animal meal, excrement, and the recovery of at least one valuable material contained in the biomass. At least the following steps are carried out in a treatment system:
  • a controlled process sequence is created in which a residue product with the at least one contained therein Recyclable material is obtained.
  • the treatment takes place in an at least two-stage process, this being done by feeding the biomass to be treated into the pyrolysis reactor and the further post-treatment of the pyrolysis coke produced there from the coke gasifier by means of thermo-chemical decomposition.
  • the gas produced in each case is burned for a combustion process in a separate burner device.
  • pollutants or additives previously contained in the biomass can be separated or disposed of and filtered out.
  • a sufficient amount of heat energy is provided, which can be used within the treatment plant for a wide variety of purposes.
  • At least a portion of the flue gas produced in the combustion device is fed to the coke gasifier to its operation for further thermal treatment of the pyrolysis coke.
  • a procedure is advantageous in which the pyrolysis gas formed in the pyrolysis reactor is collected in a collecting container immediately after it has been discharged from the pyrolysis reactor and before being passed on to the burner, and dust-like components still in the pyrolysis gas are deposited in the collecting container .
  • the pyrolysis gas formed in the pyrolysis reactor is collected in a collecting container immediately after it has been discharged from the pyrolysis reactor and before being passed on to the burner, and dust-like components still in the pyrolysis gas are deposited in the collecting container .
  • Another advantageous procedure is characterized in that the pyrolysis gas and / or the gasifier gas are or will be fed to the combustion device at a temperature of at least 400 ° C. Through the selected minimum temperature, unwanted condensation of gas components in the gas lines up to the combustion device can be avoided.
  • An alternative procedure provides that heat energy is withdrawn from the carburetor gas before it is fed into the combustion device and / or before it is fed into the internal combustion engine and is thereby cooled to a temperature value that comes from a temperature value range whose lower limit is 100 ° C., in particular 150 ° C., and its upper limit is 400 ° C., in particular 250 ° C.
  • a certain amount of thermal energy can be withdrawn from the carburetor gas before it is fed into the combustion device and / or the combustion engine, which can be used by means of the heat exchanger on a further system component provided for this purpose.
  • a variant of the method is also advantageous in which the pyrolysis gas and the gasifier gas are fed to the combustion device separately from one another.
  • the pyrolysis gas and the carburetor gas are fed to the combustion device separately from one another.
  • Another procedure is characterized in that the pyrolysis coke discharged from the pyrolysis reactor is conveyed into an intermediate container before being fed into the coke gasifier.
  • independent operation of the pyrolysis reactor and the coke gasifier can be achieved within certain limits.
  • the amount withdrawn from the intermediate container and thus the degree of filling of the coke gasifier can also be adjusted for an optimal process sequence.
  • a procedure is advantageous in which the pyrolysis coke is conveyed from the intermediate container to the coke gasifier by means of a screw conveyor and a rotary valve located downstream of the screw conveyor. This enables a controlled and safe filling of the coke gasifier to be achieved.
  • the coke gasifier comprises a screw conveyor and the pyrolysis coke conveyed further from the pyrolysis reactor is fed to the coke gasifier by means of a connecting line directly and shut off from the external ambient conditions. The treatment of the pyrolysis coke in the coke gasifier can thus be continued without a high loss of heat. In addition, long transport routes and intermediate storage can be saved.
  • Another advantageous procedure is characterized in that the flue gas diverted from the combustion device, in particular before being fed into the coke gasifier, is passed through a heat exchanger and thermal energy is withdrawn from the flue gas.
  • the thermal energy contained in the flue gas can be used and the flue gas can be cooled from 1,000 ° C to around 200 ° C, for example.
  • the saucetau shear can supply a hot water system, this thermal energy for dewatering and / or drying of the biomass can be supplied to the pyrolysis reactor before it is supplied.
  • a variant of the method is also advantageous in which the flue gas discharged from the combustion device, in particular before being fed into the coke gasifier, is passed through a filter device and is filtered in the process. In this way, suspended matter, pollutants or the like contained in the flue gas can be filtered out in order to be able to feed a cleaned flue gas to the coke gasifier for renewed combustion.
  • Another approach is distinguished when oxygen, in particular in the form of ambient air, is added to the flue gas before it is fed into the coke gasifier.
  • oxygen in particular in the form of ambient air
  • the intensity of the combustion of the flue gas in the coke gasifier can be precisely matched to the respective treatment process.
  • the higher the amount of oxygen supplied to the flue gas the more the gasification temperature or the combustion temperature can be increased.
  • a variant of the method is also advantageous in which the flue gas, which may have been enriched with oxygen, is fed to the coke gasifier at a pressure which is higher than the ambient atmospheric pressure.
  • the flue gas which may have been enriched with oxygen
  • the coke gasifier is fed from this via the connecting line to the pyrolysis reactor, in particular is fed at a pressure that is higher than the ambient atmospheric pressure.
  • a countercurrent movement with respect to the conveying direction of the pyrolysis coke in the connecting line can thus be achieved.
  • a filter effect and, associated with this, a cleaning effect of the carburetor gas can be achieved within the connection line.
  • Another approach is characterized when the pyrolysis gas and the gasifier gas fed to the pyrolysis reactor are fed together to the combustion device. A mixture of the two gases can thus be formed upstream of the combustion device. In addition, better mixing can be achieved in this way.
  • a procedure is advantageous in which the pyrolysis coke is gasified in the coke gasifier with a temperature value that comes from a temperature value range, the lower limit of which is 400 ° C., in particular 500 ° C., and the upper limit of which is 1,000 ° C., in particular 900 ° C. , is.
  • a temperature value range the lower limit of which is 400 ° C., in particular 500 ° C.
  • the upper limit of which is 1,000 ° C., in particular 900 ° C.
  • Another advantageous procedure is characterized in that the temperature value for the gasification of the pyrolysis coke in the coke gasifier is set by means of the proportion of added oxygen, in particular of mixed ambient air, to the flue gas.
  • the controlled addition of oxygen to the flue gas enables targeted control of the gasification temperature in the coke gasifier. This can counteract sintering or fusion of the residue product, which can be the case if the temperatures chosen are too high.
  • a variant of the method is also advantageous in which at least a proportion of the biomass to be treated is dewatered to a moisture value by means of a dewatering device before being fed into the pyrolysis reactor, which comes from a moisture value range, the lower limit of which is 70% by weight, in particular 80% by weight, and its upper limit is 95% by weight, in particular 90% by weight.
  • a certain amount of pre-drying of the biomass and a reduction in the water content can be achieved.
  • Another procedure is characterized by the fact that at least a proportion of the biomass to be treated is dried by means of a drying device to a moisture value that comes from a moisture value range, the lower limit of which is 3% by weight, before being fed into the pyrolysis reactor. in particular 5% by weight, and its upper limit is 20% by weight, in particular 10% by weight. This allows the moisture value to be reduced even further, which means that better and more trouble-free operation can be achieved in the subsequent pyrolysis reactor.
  • the thermal energy withdrawn from the flue gas in the heat exchanger is fed to the drying device.
  • the thermal energy contained in the flue gas can also be used when the treatment plant is in operation, without additional heat energy having to be supplied or made available.
  • Another advantageous procedure is characterized in that the mass flow of the biomass fed to the pyrolysis reactor is determined. A safer and more uniform operation of the treatment system can thus be achieved.
  • a variant of the method is also advantageous in which the biomass to be treated is fed to the pyrolysis reactor in a gas-tight manner by means of a lock system. In this way, unwanted access of oxygen into the interior of the pyrolysis reactor and thus in its treatment zone when the pyrolysis reactor is being filled can be prevented.
  • FIG. 1 shows a system diagram of a treatment system with indicated system components
  • Fig. 2 shows a further system scheme with a combined treatment unit of py rolysis reactor and coke gasifier
  • FIG. 3 shows a further possible system scheme of the treatment system according to FIG. 1, with an additional heat exchanger.
  • the same parts are provided with the same reference numerals or the same component designations, and the disclosures contained in the entire description can be transferred accordingly to the same parts with the same reference numerals or the same component names.
  • the position details chosen in the description, such as above, below, side, etc., refer to the figure immediately described and shown and these position details are to be transferred accordingly to the new position in the event of a change in position.
  • FIG. 1 a system diagram of a treatment system 1 is shown in a simplified and highly stylized manner, which comprises at least one pyrolysis reactor 2, at least one coke gasifier 3 and at least one combustion device 4.
  • the treatment system 1 is basically intended to treat biomass 5 in a thermo-chemical treatment process or thermo-chemical treatment process, the recovery of at least one valuable material contained in the biomass 5 being aimed at as one of the goals.
  • the valuable material can e.g. Phosphorus (P) or a phosphorus compound such as e.g. P2O5, potassium, calcium, magnesium or the like.
  • biomass 5 here in particular organic waste products such as sewage sludge, slaughterhouse waste, animal meal, excrement or the like are understood.
  • a first possibility is thermal recovery through incineration in waste incineration plants, a cement works or similar plants.
  • Another possibility, especially in the case of sewage sludge, is agricultural spreading in the fields. However, all of the pollutants, microplastics and the like contained in the sewage sludge are distributed across the fields and thus end up in the groundwater. Finally, composting or soil can also take place.
  • the plant components described above, namely the pyrolysis reactor 2, the coke gasifier 3 and the combustion device 4 form the basic components of the treatment plant 1 for the intended recovery of at least one valuable material contained in the biomass, where further plant components are possible and represent a supplement can.
  • At least a proportion of the biomass 5, but in particular the entire amount of biomass 5 to be treated, can be dewatered to a moisture value in a dewatering device 6 before being fed into the pyrolysis reactor 2, which comes from a moisture value range of which lower limit 70% by weight, in particular 80% by weight, and its upper limit is 95% by weight, in particular 90% by weight, based on the total mass of the biomass 5.
  • At least a proportion of the biomass 5 to be treated can be dried in a drying device 7 in a drying device 7 before being fed into the pyrolysis reactor 2 originates from a moisture range, the lower limit of which is 3% by weight, in particular 5% by weight, and the upper limit of which is 20% by weight, in particular 10% by weight.
  • the entire amount of biomass 5 to be treated is subjected to predrying. If both the dewatering device 6 and the drying device 7 are seen, they can form a drying system.
  • the biomass 5 to be treated can be fed to the pyrolysis reactor 2 with the previously described moisture reduction and / or without the previously described moisture reduction. It is still possible to determine the mass flow of the biomass 5 fed to the pyrolysis reactor 2 and, if necessary, to store or store it in a control device 8.
  • the control device 8 also serves to monitor the entire process of biomass treatment from its delivery to the end of the entire treatment process and to control all system parts or system components according to predetermined process steps.
  • the respective communication connections between the control device 8 and the individual system parts or system components are indicated in dashed lines.
  • the feeding of the biomass 5 into the pyrolysis reactor 2 can take place in a preferably gas-tight manner by means of a lock system 9, such as a vertical rotary lock.
  • thermo-chemical conversion of the biomass 5 takes place in it, which can be referred to as a pyrolysis process.
  • a thermo-chemical conversion of the biomass 5 takes place in it, which can be referred to as a pyrolysis process.
  • thermal decomposition of the biomass 5 in pyrolysis coke and pyrolysis gas each with a wide variety of components.
  • the pyrolysis coke is predominantly a solid fraction, which can also be referred to as carbonizate.
  • the pyrolysis reactor 2 can for example be designed as a screw reactor in which the thermal decomposition of the biomass 5 takes place at a temperature in a temperature range between 400 ° C, in particular 450 ° C, and 600 ° C, in particular 550 ° C. This process takes place under reduced oxygen conditions with a residence time between 20 and 30 minutes. There can be a low oxygen concentration of less than 5% in the pyrolysis reactor 2.
  • the pyrolysis gas produced is mostly an oil / gas mixture, possibly with dust-like fractions.
  • the pyrolysis coke produced in the process and the pyrolysis gas are discharged or diverted from the pyrolysis reactor 2 in a spatially separated manner.
  • the further treatment of the pyrolysis coke with the possible process steps is described below.
  • the pyrolysis coke formed in the pyrolysis reactor 2 from the biomass 5 is now in principle Lich to carry out a further treatment step in the coke gasifier 3 facedgeför changed. This can be done in a direct way. However, it would still be possible for the pyrolysis coke discharged from the pyrolysis reactor 2 to be conveyed into an intermediate container 10 before being fed into the coke gasifier 3 and temporarily stored there.
  • the removal from the intermediate container 10 or the step of further conveying the pyrolysis coke from the intermediate container 10 to the coke gasifier 3 can e.g. take place by means of a screw conveyor and a rotary valve arranged after the screw conveyor.
  • the pyrolysis coke is further gasified in a subsequent treatment step.
  • the pyrolysis coke is decomposed into a predominantly solid residue product, in particular a free-flowing residue product, and into a gasifier.
  • the mostly solid residue product contains the at least one valuable material on which the recovery is directed.
  • the residue product is spatially separated from the coke gasifier 3 discharged from the gasifier gas, whereby the residue product can be collected in an unspecified container.
  • the gasifier gas is thus derived specifically from the coke gasifier 3.
  • the pyrolysis gas produced in the pyrolysis reactor 2 from the biomass 5 is in turn passed into the combustion device 4, the pyrolysis gas being burned in the combustion device 4 with the formation of a flue gas.
  • the resulting or formed flue gas is diverted from the combustion device 4.
  • both gases namely the pyrolysis gas and the carburetor gas, are fed to the combustion device 4, they can be fed to the combustion device 4 spatially separated from one another and burned therein. Independently of this, however, both gases could also be fed together to the combustion device 4, as is indicated by an arrow shown in dash-dotted lines.
  • the combustion gas produced during the operation of the internal combustion engine 11 could also be mixed with the flue gas fed to the coke gasifier 3. However, it would also be possible not to feed a portion of the flue gas diverted from the combustion device 4 to the coke gasifier 3, but rather either before it is passed through a filter device 13 and / or a heat exchanger 14 or after passing through the filter device 13 and / or the heat exchanger 14 for another thermal use. This can be for a wide variety of purposes, such as another combustion process, in a drying system, as a recirculation gas or the like.
  • a further possible partial amount of the flue gas can e.g. take place before the heat exchanger 14 and / or after the heat exchanger 14.
  • a portion of the flue gas is removed after the heat exchanger 14 and before the filter device 13 and fed to the combustion device 4 again.
  • the feed line can e.g. take place before entry into the combustion device 4 in such a way that the partial amount of smoke gas is mixed with the pyrolysis gas and the two gases are fed together to the combustion device 4.
  • a further partial amount of the flue gas could also be removed after passing through the filter device 13.
  • This further possible part of the flue gas can be used in the drying device 7 as heat energy carriers during the drying process.
  • the previously described removal of at least a partial amount from the total flow of the total amount of flue gas can take place, but does not have to be. It would also be possible to feed the entire flow of flue gas, that is, the entire amount of flue gas to the coke gasifier 3. If at least a partial amount or several partial amounts are withdrawn, this exemplary embodiment shown can be a maximum of four partial amounts and their withdrawal from the total amount or the total flow.
  • a first partial amount must always be fed to the coke gasifier 3 in any case.
  • the other subsets can be those which are supplied to the drying device 7, the combustion device 4 and the chimney 15. It should be mentioned that only one of the subsets described above can be withdrawn, or two subsets or even three subsets can be withdrawn.
  • the chimney 15 is schematically seen in the flow direction of the flue gas to the coke gasifier 3, a admixing device 16 for additional oxygen arranged upstream of the flue gas.
  • the purpose of the admixing device 16 is explained in more detail below.
  • the pyrolysis gas formed or arising in the pyrolysis reactor 2 can be collected in a collecting container 12 immediately after it has been discharged from the pyrolysis reactor 2 and before it is passed on to the combustion device 4. This creates the possibility, while it is in the collecting container 12, that dust-like fractions that are still in the pyrolysis gas can be deposited in the collecting container 12.
  • the pyrolysis gas consists predominantly of approx. 15-20% permanent gases and in addition each 100% of approx. 85-80% condensable components.
  • the permanent gases can in particular be CO, CO2, H2, N2, H2S, CH4.
  • the condensable components can primarily be H2O, organic compounds such as acetic acid, butyric acid, aromatic hydrocarbons, diverse hetero compounds or compounds of higher molecular weight (oils) or the like.
  • the pyrolysis gas and / or the carburetor gas are or will be fed to the combustion device 4 at a temperature of at least 400 ° C. If the temperature in the supply lines is lower, this can lead to unwanted condensation in the line or in the lines.
  • the gas diverted from the combustion device 4 is generally referred to as “flue gas”.
  • flue gas the combustion product formed or arising during the joint combustion is referred to below as "flue gas" when both the pyrolysis gas and the gasifier gas are fed into the Brennvor direction 4.
  • the combustion product "flue gas” still has a residual proportion of oxygen (O2), whereby the oxygen content in the flue gas can be around 5%.
  • the flue gas is diverted from the combustion device 4, at least a portion of which is subsequently fed to the coke gasifier 3. It can thus be advantageous if the flue gas derived from the Brennvor device 4 is filtered in the filter device 13, in particular before being fed into the coke gasifier 3.
  • this oxygen in particular in the form of ambient air, can be added or buried before the flue gas is fed into the coke gasifier 3. This can be done by means of the admixing device 16.
  • the operating temperature of the coke gasifier 3 can subsequently be set within certain limits through the amount or proportion of added oxygen to the flue gas, and thus the temperature of the gasification of the py rolyse coke in the coke gasifier 3 can be determined.
  • the pyrolysis coke can be gasified in the Koksverga ser 3 with a temperature value which comes from a temperature value range whose lower limit is 400 ° C, in particular 500 ° C, and whose upper limit is 1,000 ° C, in particular 900 ° C.
  • the flue gas discharged from the combustion device 4 mostly has a very high temperature, e.g. between 800 ° C and 1,200 ° C, in particular from 1,000 ° C.
  • the flue gas derived from the combustion device 4 in particular before being fed into the coke gasifier 3, can be passed through the heat exchanger 14.
  • a portion of the thermal energy contained in the flue gas can be withdrawn.
  • the withdrawn heat energy of the drying device 7 for dehumidification and drying of the biomass to be treated 5 before being fed into the pyrolysis Re actuator 2 and thus used to reduce the moisture.
  • FIG. 2 shows and describes an embodiment variant of the treatment system 1 described in detail in FIG. 1 and the process steps that differ slightly therefrom or the process sequence that differs slightly therefrom.
  • the same reference numerals or component names as in the previous FIG. 1 are used for the same parts. In order to avoid unnecessary repetition, reference is made to the detailed description in the preceding FIG. 1.
  • the system structure of the treatment system 1 basically corresponds to that arrangement as shown and described in FIG. Therefore, a detailed description of the other parts of the system or system components is not given here. The description is to be transferred analogously from FIG. 1 to the embodiment shown.
  • the coke gasifier 3 comprises a screw conveyor or is provided with it or is designed as a screw conveyor. This is shown schematically simplified.
  • the coke gasifier 3 is preferably arranged below the pyrolysis reactor 2 and is in flow connection with it directly via its own connecting line 17.
  • the connecting line 17 can for example be designed as a pipe in the form of a case shaft.
  • the discharge area of the pyrolysis reactor 2 is thus in direct conveying or flow connection with the supply area of the coke gasifier 3.
  • the connection line 17 connects the interior of the pyrolysis reactor 2 directly with the interior space of the coke gasifier 3. This means that the pyrolysis coke conveyed on from the pyrolysis reactor 2 can be conveyed or fed to the coke gasifier 3 while closing off the external ambient conditions.
  • the flue gas diverted from the combustion device 4, in particular before being fed into the coke gasifier 3, is passed through a filter device 13 and filtered in the process.
  • oxygen in particular in the form of ambient air, can be added to the flue gas before it is fed into the coke gasifier 3.
  • the flue gas optionally enriched with oxygen, can preferably be fed to the coke gasifier 3 at a pressure which is higher than the ambient atmospheric pressure.
  • the feed line into the interior of the coke gasifier 3 can be fed to only one feed line position or also to several feed line positions arranged distributed over the longitudinal extent.
  • the at least one feed line position is preferably arranged in a longitudinal section at the end of the coke gasifier 3.
  • the pyrolysis coke further treated in the coke gasifier 3 is forcibly conveyed further within the coke gasifier 3 from the supply area to the discharge area by the provision of the screw conveyor.
  • This forced conveying movement By means of this forced conveying movement, better mixing and treatment of the pyrolysis coke in the coke gasifier 3 can also be achieved.
  • the connecting line 17 has a predominantly low to completely vertical alignment.
  • the coke gasifier housing can be designed as a hollow cylinder and thus as a tube.
  • the longitudinal axis of the coke gasifier housing can preferably be oriented in an inclined manner with respect to a horizontal plane. The rising incline refers to the slope starting from the supply area towards the discharge area of the coke gasifier 3.
  • thermo-chemical treatment of the biomass 5, which can also be referred to as gasification material, takes place by feeding the flue gas, which may be enriched with oxygen, into the interior of the coke gasifier 3.
  • the biomass 5 e.g.
  • plastics and / or plastic composites can also be thermally treated in the treatment system 1 and pyrolysis gas and pyrolysis coke can be formed therefrom.
  • the gasifier gas is passed or pressed into the interior of the pyrolysis reactor 2 via the connecting line 17. This takes place in the countercurrent principle with respect to the conveying direction of the pyrolysis coke, in particular with a special pressure with respect to the ambient atmospheric pressure.
  • the pyrolysis coke located in the connecting line 17 serves as a filter through which the gasifier gas must flow.
  • the pyrolysis gas and the gasifier gas fed to the pyrolysis reactor 2 are then derived together from the interior of the pyrolysis reactor 2 and fed to the combustion device 4.
  • FIG. 3 is a further possible embodiment variant of the treatment system 1 previously described in detail in FIG. 1 and the process steps that differ slightly therefrom or the process sequence that differs slightly therefrom is shown and described.
  • the same reference numerals or component designations as in the preceding FIGS. 1 and 2 are again used for the same parts. In order to avoid unnecessary repetition, reference is made to the detailed description in the preceding FIGS. 1 and 2.
  • the system structure of the treatment system 1 basically corresponds to that arrangement as shown and described in FIG. 1. Therefore, the detailed description of the other parts of the system or system components is not given here. The description is to be transferred analogously from FIG. 1 to the embodiment shown here. It should be mentioned that the coke gasifier 3 can, independently of this, also be designed as it was previously described and shown in detail in FIG.
  • the gasifier gas diverted from the coke gasifier 3 separately from the residue product is in this embodiment before it is fed into the combustion device 4 and / or into the internal combustion engine 11 through a further heat exchanger 18 and thus a predetermined amount of heat is extracted from the gasifier gas.
  • This intended reduction in the temperature of the carburetor gas is supplied to the Brennvorrich device 4 and / or the internal combustion engine 11 at a lower temperature.
  • the temperature value of the cooled gasifier gas can originate or be selected from a temperature value range whose lower limit is 100 ° C., in particular 150 ° C., and whose upper limit is 400 ° C., in particular 250 ° C.
  • a particularly preferred temperature value or temperature value range can e.g. 200 ° C ⁇ 20 ° C.
  • This heat energy withdrawn from the gasifier gas by the further heat exchanger 18 can, for example, also be fed to the drying device 7 for dehumidifying and drying the biomass 5 to be treated before being fed into the pyrolysis reactor 2 and thus used to reduce the moisture.
  • other system components can also be supplied with this thermal energy.
  • return lines from the drying device 7 to the heat exchangers 14, 18, which have not been described in more detail before, are indicated and identified with the Roman numerals “I” and “II”.
  • the line “I” here connects the first heat exchanger 14 to the drying device 7, with the other Line “II” also connects the further heat exchanger 18 with the drying device 7.
  • drying device 7 it would also be possible, in addition to or instead of the drying device 7, to supply the heat energy withdrawn from the heat exchanger (s) 14, 18 with appropriate line connections. Usually a closed circuit with supply lines and return lines is provided. Since this is considered to be generally known, the detailed illustration is omitted for the sake of clarity.
  • an actuator 19 is indicated in the line connection between the admixing device 16 and the coke gasifier 3, which is possibly in communication with the control device 8.
  • the actuator 19 can e.g. be formed by a switching valve or the like.
  • the flue gas can also be enriched with a certain proportion of oxygen, in particular in the form of ambient air.
  • the pyrolysis coke in the Koksverga ser 3 can be gasified with a temperature value that comes from a temperature range whose lower limit is 400 ° C , in particular 500 ° C, and its upper limit is 1,000 ° C, in particular 900 ° C.
  • the oxygen-enriched flue gas and / or the oxygen, in particular in the form of ambient air can preferably be fed to the coke gasifier 3 at a pressure that is higher than the ambient atmospheric pressure.
  • a pressure-increasing element is shown schematically simplified.
  • the coke gasifier 3 generally described above can be designed or configured, for example, as a fixed bed, fluidized bed, screw or rotary tube reactor.
  • All information on value ranges in the objective description are to be understood in such a way that they include any and all sub-ranges, e.g.
  • the indication 1 to 10 is to be understood in such a way that all sub-areas, starting from the lower limit 1 and the upper limit 10, are included, i.e. all subranges start with a lower limit of 1 or greater and end at an upper limit of 10 or less, e.g. 1 to 1.7, or 3.2 to 8, 1, or 5.5 to 10.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

L'invention concerne un procédé pour le traitement thermochimique de biomasse (5) et le recyclage d'une matière de valeur contenue dans celle-ci. La biomasse (5) est fournie à un réacteur de pyrolyse (2) et décomposée dans celui-ci en coke de pyrolyse et en gaz de pyrolyse, le coke de pyrolyse étant ensuite transporté à un gazéificateur de coke (3) et décomposé dans celui-ci en un produit résiduel solide et un gaz de gazéificateur. Le gaz de pyrolyse et le gaz de gazéificateur sont conduits à un dispositif de combustion (4) et brûlés dans celui-ci en gaz de fumée. Au moins une partie du gaz de fumée du dispositif de combustion (4) étant conduite au gazéificateur de coke (3).
EP20718519.0A 2019-03-06 2020-03-04 Procédé pour le recyclage d'au moins une matière de valeur contenue dans une biomasse Withdrawn EP3969545A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
ATA50176/2019A AT522257A1 (de) 2019-03-06 2019-03-06 Verfahren zur Rückgewinnung zumindest eines in einer Biomasse enthaltenen Wertstoffes
ATA50707/2019A AT522258A1 (de) 2019-03-06 2019-08-09 Verfahren zur Rückgewinnung zumindest eines in einer Biomasse enthaltenen Wertstoffes
PCT/AT2020/060062 WO2020176917A1 (fr) 2019-03-06 2020-03-04 Procédé pour le recyclage d'au moins une matière de valeur contenue dans une biomasse

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WO2019188691A1 (fr) 2018-03-30 2019-10-03 三井・ダウ ポリケミカル株式会社 Composition de résine pour produit d'étanchéité, matériau de couvercle, et emballage
CN113293015A (zh) * 2021-06-25 2021-08-24 王晓光 一种秸秆快速制炭及烟气烟尘回收处理装置及方法
CN114874815B (zh) * 2022-04-29 2024-02-27 东南大学 一种高含水中药渣气化制备高品质合成气的装置及方法

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US4794871A (en) * 1985-08-19 1989-01-03 Environment Protection Engineers, Inc. Method and installation for the treatment of material contaminated with toxic organic compounds
WO2002083815A1 (fr) * 2001-04-12 2002-10-24 Fenner, Hans, Rudolf Installation et procede pour produire de l'energie par pyrolyse
DE102007041624A1 (de) * 2007-09-03 2009-03-05 Technische Universität Dresden Verfahren und Anlage zur Erzeugung eines teerarmen Brenngases
DE102008028241A1 (de) 2008-06-16 2009-12-17 G & A Industrieanlagen Gmbh Vorrichtung zur thermochemischen Umwandlung von Biomasse
EP3309240A1 (fr) * 2016-10-12 2018-04-18 WS-Wärmeprozesstechnik GmbH Procédé et dispositif de gazéification de biomasse

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