EP2655552A1 - Procédé de pyrolyse d'une matière d'alimentation organique - Google Patents

Procédé de pyrolyse d'une matière d'alimentation organique

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Publication number
EP2655552A1
EP2655552A1 EP10805202.8A EP10805202A EP2655552A1 EP 2655552 A1 EP2655552 A1 EP 2655552A1 EP 10805202 A EP10805202 A EP 10805202A EP 2655552 A1 EP2655552 A1 EP 2655552A1
Authority
EP
European Patent Office
Prior art keywords
pyrolysis
reactor
gas
heated
reforming
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Withdrawn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
EP10805202.8A
Other languages
German (de)
English (en)
Inventor
Prerak Goel
Christopher THANNHÄUSER
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.)
Thannhaueser Goel IP AG
Original Assignee
Thannhaueser Goel IP AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Thannhaueser Goel IP AG filed Critical Thannhaueser Goel IP AG
Publication of EP2655552A1 publication Critical patent/EP2655552A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C10B49/18—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form according to the "moving bed" type
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • 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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • 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
    • C10J3/06—Continuous processes
    • C10J3/12—Continuous processes using solid heat-carriers
    • 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
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • 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
    • C10J2300/1853—Steam reforming, i.e. injection of steam only
    • 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
    • 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
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • 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
    • C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention relates to a process for pyrolysis of hydrous organic feedstock, in particular of organic waste and biomass, with the following process steps: a) a lumped inert heat transfer medium circulated in the circuit is heated in a preheater, b) the heated heat transfer medium is mixed with the hydrous feedstock c) in the pyrolysis reactor, the feedstock is optionally pyrolyzed with further addition of steam, d) the mixture of pyrolysis gas and water vapor formed in the pyrolysis reactor is reformed in a reforming reactor into a product gas having a high hydrogen content (first end product), e) the pyrolysis coke formed in the pyrolysis reactor (second end product) is discharged out of the pyrolysis reactor together with the heat carrier and separated from the heat carrier, and f) the separated heat carrier is returned to the preheater.
  • Such a method is known, for example, from EP 1 337 607 and embodied in the appendix "Blauer Turm" (see www.blue-tower.de).
  • knew method is the heat carrier, the z. B. may consist of heat-resistant ceramic balls, heated in the preheater with the aid of flue gas from a furnace to about 1100 ° C and entered in this state via a solids lock in the reforming reactor located below the preheater to there the heat required for the reforming in the enter required temperature range.
  • the heat transfer medium cools down to the temperature level required for heating the pyrolysis reactor (about 750 ° C.) and is in turn introduced via a metering device into the pyrolysis reactor underneath, to which the feed material is simultaneously supplied.
  • the heat transfer medium then passes through the pyrolysis reactor together with the feedstock and, together with the pyrolysis coke produced during the pyrolysis, is discharged from the bottom of the pyrolysis reactor at a temperature of about 600.degree.
  • the heat carrier is then conveyed by means of an elevator up and entered via a lock again from above into the preheater. If the amount of water added to the hydrous feed is insufficient to reform, steam is also added to the pyrolysis reactor.
  • the system inevitably has a relatively large overall height due to the guidance of the heat transfer circuit, so that the heat transfer medium for the return to the preheater must be lifted over a relatively long conveying path, which is unfavorable both energetically and wear.
  • the heat transfer medium must be heated in the preheater up to 1100 ° C, ie up to the range of bright yellow heat, whereby the life of the one part of the heat carrier and the other part of the heat carrier leading plant parts, especially the solids sluices, can be greatly affected.
  • the invention proposes starting from the method of the type mentioned above, g) that the reforming reactor is arranged separately from the heat transfer circuit and is heated separately from this.
  • the heat transfer circuit comprises only the preheater and the pyrolysis reactor.
  • the necessary height of the plant is reduced by about the height of the reforming reactor. Because of the reduced height, the delivery path for the return of the heat carrier is shortened accordingly.
  • the reforming process can be controlled much more precisely with regard to optimized product discharge (product gas or pyrolysis coke) and optimized for the highest possible hydrogen content in the product gas.
  • a first, expedient embodiment of the invention provides that a subset of the product gas is diverted and is burned in a gas burner whose flue gas first heats the reforming reactor and then the heat carrier in the preheater.
  • the process remains energy self-sufficient and enables optimized application to pyrolysis coke. This is particularly important in locations where the pyrolysis in agriculture z. B. is needed for soil improvement.
  • a second expedient embodiment of the invention provides that the entire pyrolysis coke or a separated subset of the pyrolysis coke is incinerated in a coke furnace whose flue gas first heats the reforming reactor and then the heat carrier in the preheater. Again, the process remains energy self-sufficient and allows optimized application of hydrogen-containing pyrolysis gas. This is especially important in locations where z. B. wants to generate electricity with a gas turbine or a gas engine, z. B. to fill the power generation gaps of electricity generating solar systems.
  • the reforming process can in both cases - regardless of the particular energy source - take place in an externally heated reaction chamber of the reforming reactor. This has the advantage that the reforming process can be accomplished alone in the gas phase without interference by passing solids, if necessary in the presence of a catalyst which is located in the reaction space of the reforming reactor. Due to the presence of a suitable catalyst, it is known that the reforming process can be considerably intensified.
  • the reforming process can also be carried out in a moving bed reactor, the circulating high-temperature heat transfer medium first by the flue gas of the gas burner and / or the coke firing heated preheating and then one of them through a solids sluice separated reaction chamber, the from flows through to be reformed pyrolysis gas.
  • a catalyst which is not polluted by the feedstock and can optionally be thermally, chemically or mechanically reactivated outside the reforming reactor or can be completely or partially replaced.
  • the preheater upstream of the pyrolysis reactor is subdivided into two preheating chambers, which are successively passed through by the heat transfer medium and of which the one from the pyrolysis gas passed through and the other from the passed flue gas from the Reforming reactor is heated.
  • the preheating chamber of the moving bed reactor may also be subdivided into two preheating chambers, which are successively passed through by the high-temperature heat carrier and one of which heats the product gas passing through it and the other from the flue gas of the gas burner and / or coke firing becomes.
  • Fig. 1 Schematically the method according to the
  • a preheater with the reference numeral 1 a pyrolysis reactor with the reference numeral 2 and a reforming reactor with the reference numeral 3 are designated. Furthermore, the plant comprises a gas burner 4, a sieve 5, a product gas purification 6 and a steam generator 7.
  • the heat carrier 8 is formed by refractory ceramic balls, which are located for the most part in bulk in the preheater 1 and the pyrolysis reactor 2.
  • the heat transfer medium 8 is circulated continuously and moves slowly from top to bottom first through the preheater 1 and then through the pyrolysis reactor 2, then as Siebrückhalt on the screen 5 and an elevator 9 back up into the preheater. 1
  • gas-tight solids sluices 10 are provided for the passage of the heat carrier 8.
  • the heat transfer medium 8 is heated in the preheater 1 to about 800 ° C and entered at this temperature from above into the pyrolysis reactor 2. At the same time with the heat transfer medium 8 is in the pyrolysis reactor 2 via an adding device 11 to be pyrolyzed water-containing organic feedstock in the form of organic waste or biomass input.
  • air or oxygen or a mixture of air and oxygen may be introduced into the pyrolysis reactor by means of an adding device 12.
  • this feedstock On its way through the pyrolysis reactor 2, this feedstock is pyrolyzed with the addition of water vapor.
  • the energy required for the pyrolysis provides the heat transfer medium 8, which accordingly cools in the pyrolysis reactor 2 from 800 ° C to 600 ° C. If air and / or oxygen are added, a stoichiometric combustion of carbon also takes place in the pyrolysis reactor 2, whereby optionally additional heat is introduced into the pyrolysis reactor.
  • the pyrolysis coke formed during the pyrolysis is discharged together with the heat transfer medium 8 via a discharge device 14 arranged downstream of the pyrolysis reactor 2 together with the heat transfer medium 8 and applied to the screening plant 5.
  • the heat carrier 8 is retained as Siebrückhalt and fed to the elevator 9, which promotes the heat carrier 8 upwards and enters from above through the solids lock 10 in the preheater 1.
  • the pyrolysis coke separated off as a screen pass is conveyed to a product dispenser 15 where it is dispensed as the first product of the process.
  • the above emerging from the pyrolysis reactor 2 pyrolysis gas-steam mixture is entered into a heated from the outside, separate reaction chamber 16 of the reforming reactor 3 and there subjected to the reforming process.
  • the heating of the reaction chamber 16 of the reforming reactor 3 via a reaction chamber 16 surrounding the heating jacket 17 which is flowed through by the hot flue gas of about 1100 ° C of the gas burner 4 and the reaction chamber 14 is heated accordingly.
  • the product gas produced in the reaction chamber 16 by reforming is purified in the product gas purification unit 6 and sent to a product gas outlet 8 as a second process product.
  • the fuel required for the operation of the gas burner is a partial flow of the product gas which is supplied to the gas burner 4 via a gas line 19.
  • the gas burner 4 is further associated with an air supply 20, via which the gas burner is supplied with air.
  • the amount of flue gas and flue gas temperature generated in the gas burner 4 can be controlled very accurately, whereby it is possible to precisely control the heat supplied to the reaction chamber 16 of the reforming reactor 3.
  • a part of the exhaust gas stream can also be recycled into the furnace. In this way, one can advantageously return a portion of the sensible heat from the exhaust gas to the process.
  • the exhaust gas from the heating jacket 17 is supplied via an exhaust pipe 21 to the preheater 1 to its heating.
  • This exhaust still has a temperature of about 860 ° C, which is sufficient to heat the heat carrier located in the preheater 1 8 to the required about 750 ° C.
  • steam is additionally introduced into the pyrolysis reactor 2.
  • This additional steam is generated in a steam generator 7, which is expediently heated with the exhaust gas 22 from the preheater 1.
  • the additional steam generated in the steam generator 7 is input via a steam line 23 from below into the pyrolysis reactor 2.
  • the amount of steam can be controlled by the fact that the steam generator 7 via a water supply valve 24, a targeted amount of water is supplied.
  • a coke firing 34 which can be heated via a Kokstechnisch 37 with the pyrolysis or a subset of the pyrolysis coke produced.
  • the heating with product gas shown in FIG. 1 and the heating with pyrolysis coke shown in FIG. 2 can also be combined with one another so that the system can be combined with product gas, pyrolysis coke or combined heating with both heating means.
  • the reforming reactor 3 is designed as a moving bed reactor, which operates with a circulating high-temperature heat carrier 40, which consists of particularly temperature-stable ceramic balls, first in one of the flue gas of a gas burner (cf., the gas burner 4 shown in Figure 1) / or a coke-firing (cf the coke-fired furnace 34 of Figure 2) are heated and thereafter pass through a reaction chamber 42 through which the pyrolysis-gas-vapor mixture flows in order to release the heat absorbed in the preheating chamber 41, and then into the furnace via an elevator 43 Voricarmhunt 41 to be returned. Because the high-temperature heat carrier 40 comes into contact exclusively with gases here, there are hardly any disturbing solids in the moving bed reactor or at its high-temperature heat carrier 40, so that the reforming process can be controlled very precisely.
  • a gas burner cf., the gas burner 4 shown in Figure 1
  • a coke-firing cf the coke-fired furnace 34 of Figure 2
  • the flue gas used for the heating of the reforming reactor is then fed to the preheater 1 of the pyrolysis reactor 2.
  • the embodiment according to FIG. 4 additionally deals with the problem of using the sensible heat from the product gas.
  • the preheater 1 resulting from FIG. 1 has been subdivided into two preheating chambers 1a and 1b. Both preheat chambers 1a and 1b are passed through by the heat carrier 8 and are connected to each other by a solids sluice.
  • the preheating chamber 1a is - as in the embodiment of Figure 1 - heated by the flue gas from the heating jacket 17 of the reforming reactor 3.
  • the preheating chamber 1b is heated by the product gas flowing through it, which senses its sensible heat the heat carrier 8 delivers and only then the product gas cleaning 6 is supplied.
  • FIG. 5 An alternative to the use of sensible heat from the product gas is shown in FIG 5.
  • the resulting from Figure 3 preheating 41 of the moving bed reactor has been divided into two Vormérmhuntn 41 a and 41 b, which are separated from each other by a solids sluice and are traversed by the high-temperature heat transfer 40 ,
  • the preheating chamber 41a is heated by the flue gas of the coke firing 34 as in the exemplary embodiment according to FIG. 3, while the preheating chamber 41b is heated by the product gas which is supplied via a connecting line 44 between the reaction chamber 42 and the preheating chamber 41b and then via a connecting line 45 the product cleaning 6 is supplied.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé de pyrolyse de matière d'alimentation organique contenant de l'eau, en particulier de déchets organiques et de biomasse, avec les étapes de procédé suivantes : - un caloporteur (8) inerte, en morceaux, circulant dans un circuit, est chauffé dans un préchauffeur (1), - le caloporteur (8) chauffé est introduit dans un réacteur de pyrolyse (2) simultanément avec la matière d'alimentation contenant de l'eau, - dans le réacteur de pyrolyse (2), la matière d'alimentation est pyrolysée éventuellement avec une addition supplémentaire de vapeur d'eau, - le mélange de gaz de pyrolyse et de vapeur d'eau formé dans le réacteur de pyrolyse (2) est réformé dans un réacteur de reformage (3) en un produit gazeux ayant une teneur en hydrogène élevée (premier produit final), - le coke de pyrolyse (2) formé dans le réacteur de pyrolyse est évacué conjointement avec le caloporteur (8) provenant du réacteur de pyrolyse (2) et séparé du caloporteur, et - le caloporteur (8) séparé est ramené dans le préchauffeur (1). L'invention vise, dans ce procédé, à diminuer la hauteur de l'installation et à éviter des températures élevées gênantes dans la région du circuit du caloporteur. A cet effet, le réacteur de reformage (3) est disposé séparément du circuit du caloporteur et est chauffé séparément de celui-ci.
EP10805202.8A 2010-12-20 2010-12-20 Procédé de pyrolyse d'une matière d'alimentation organique Withdrawn EP2655552A1 (fr)

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PCT/EP2010/007798 WO2012083979A1 (fr) 2010-12-20 2010-12-20 Procédé de pyrolyse d'une matière d'alimentation organique

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EP2655552A1 true EP2655552A1 (fr) 2013-10-30

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DE102021134442B4 (de) 2021-12-23 2023-07-06 Concord Blue Patent Gmbh Anlage zur Erzeugung eines Synthesegases und Verfahren zum Betreiben derselben

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DE19755693C1 (de) * 1997-12-16 1999-07-29 Dmt Gmbh Verfahren zur Vergasung von organischen Stoffen und Stoffgemischen
DE19945771C1 (de) * 1999-09-24 2001-02-22 Muehlen Gmbh & Co Kg Dr Verfahren zur Vergasung von organischen Stoffen und Stoffgemischen
DE10055360B4 (de) 2000-11-08 2004-07-29 Mühlen, Heinz-Jürgen, Dr.rer.Nat. Verfahren zur Vergasung von flüssigen bis pastösen organischen Stoffen und Stoffgemischen
FI20030241A (fi) * 2003-02-17 2004-08-18 Fortum Oyj Menetelmä synteesikaasun tuottamiseksi
DE102007005799B4 (de) * 2006-10-18 2018-01-25 Heinz-Jürgen Mühlen Verfahren zur Erzeugung eines wasserstoffreichen Produktgases
WO2010137028A2 (fr) * 2009-05-28 2010-12-02 Concord Blue Technology Pvt. Ltd. Procédé pour générer de l'énergie à partir de matières organiques et/ou de biomasse

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See references of WO2012083979A1 *

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