WO2020058093A1 - Procédé pour l'oxydation partielle de produits de dégradation générés par pyrolyse pour produire un gaz de synthèse dans un réacteur à courant continu - Google Patents

Procédé pour l'oxydation partielle de produits de dégradation générés par pyrolyse pour produire un gaz de synthèse dans un réacteur à courant continu Download PDF

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Publication number
WO2020058093A1
WO2020058093A1 PCT/EP2019/074408 EP2019074408W WO2020058093A1 WO 2020058093 A1 WO2020058093 A1 WO 2020058093A1 EP 2019074408 W EP2019074408 W EP 2019074408W WO 2020058093 A1 WO2020058093 A1 WO 2020058093A1
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WIPO (PCT)
Prior art keywords
synthesis gas
biomass particles
reactor
oxidation
solid biomass
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.)
Ceased
Application number
PCT/EP2019/074408
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German (de)
English (en)
Inventor
Leonhard Baumann
Roland Möller
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.)
Ecoloop GmbH
Original Assignee
Ecoloop 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
Application filed by Ecoloop GmbH filed Critical Ecoloop GmbH
Priority to CN201980060770.6A priority Critical patent/CN112703245A/zh
Priority to EP19770016.4A priority patent/EP3853326A1/fr
Publication of WO2020058093A1 publication Critical patent/WO2020058093A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • 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
    • C10J3/02—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
    • 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
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • 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
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • 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
    • C10J2300/0989—Hydrocarbons as additives to gasifying agents to improve caloric properties
    • 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
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • 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 method for producing synthesis gas from solid biomass particles and synthetic carbon-rich substances using a direct current reactor according to the preamble of claim 1.
  • Plastic waste in particular is becoming an increasing threat to the environment, especially in developing countries and in the world's oceans. Garbage collection has become increasingly established in industrialized and emerging countries.
  • the low energy efficiency in the generation of electricity from waste incineration plants is based on the problem that such incineration plants are only suitable for generating steam, the steam temperature and thus also the steam pressure also having to be kept relatively low due to the high-temperature corrosion which is triggered by the chlorine in the waste. This results in a very low efficiency in electricity generation using classic steam turbines, so that a large part of the energy generated can only be used as low-temperature heat.
  • DE102007062414B4 proposes a method that provides for the gasification of carbon-rich substances in a lime-bed. Although the efficiency could be increased significantly by generating a purified synthesis gas, however, such systems are also of a size that also require a considerable amount of transport for the input materials. Another disadvantage is that a large-scale lime bed has to be circulated with a high level of equipment.
  • gasification technologies are also known, which can also be implemented on a smaller scale using small de-local plants.
  • these are mostly technologies that use biomass, such as wood chips or wood pellets, as input material.
  • biomass such as wood chips or wood pellets
  • Such a method is disclosed for example in EP1436364B1.
  • Such processes have the sole aim of generating energy because, due to their specific process and control concepts, they have so far only been able to process wood or other biomass materials.
  • waste recycling for example the recycling of synthetic plastic waste.
  • the calorific value of the input materials was previously limited to a low level, which is usual for biomass, so that the resulting wood gas also has a low energy density.
  • the object of the present invention is therefore a method
  • This object is achieved according to the invention in that a partial oxidation of pyrolytically produced fission products for the production of synthesis gas is carried out in a direct current reactor through which solid biomass particles flow, with synthetic carbon-rich substances being admixed with the solid biomass particles.
  • the solid biomass particles are used in a drying zone and in a subsequent pyrolysis zone as a migrating reaction surface for the pyrolytic cleavage of the synthetic carbon-rich substances.
  • the oxygen chemically bound in the solid biomass particles serves at least partially as an oxidizing agent for the partial oxidation, an additional supply of oxygen-containing gas taking place in an oxidation zone, as a result of which the biomass particles and the synthetic, carbon-rich substances are wholly or partly in finely divided
  • Oxidation residues are converted with a particle size such that they are aerosol capable.
  • Wood as a rule, is an example of a synthetic carbon-rich substance that can also only form aerosol-capable oxidation residues, polystyrene.
  • a preferred embodiment of the method consists in that the synthesis gas quantity generated in a single DC reactor corresponds to a thermal output of 10 to 2000 kW, preferably a thermal output of 10 to 1000 kW and particularly preferably a thermal output of 10 to 500 kW.
  • decentralized solutions can be found in different ways, preferably at the waste sites
  • Intake amount of a synthesis gas extraction device is specified. This practically pulls a certain amount of gas through the DC reactor, which is ultimately feeds from the oxygen-containing gas from the oxidation zone and is supplemented in the further course of the process by gaseous reaction and fission products due to the physico-chemical processes.
  • the admixture of synthetic carbon-rich substances requires special control of the method according to the invention, in that the dosage of the synthetic carbon-rich substances is designed in such a way that it forms in a
  • Equilibrium ratio of gasified solid biomass particles and gasified synthetic carbon-rich substances a proportionate gasification of 20% to 80%, preferably from 20% to 50% and particularly preferably from 20% to 30% of the solid
  • Biomass particles based on the total dosed mass fraction of solid biomass particles and synthetic carbon-rich substances. This control is essential for the functioning of the process, there is one
  • the process can be advantageously designed in that the finely divided oxidation residues, after having passed through a reduction zone, are at least partially discharged as aerosol as dust-like constituents together with the resulting synthesis gas stream.
  • the oxidation residues are at least partially discharged via the bottom of the ash bunker at the lower end of the DC reactor via a discharge device. If the oxidation residues are not aerosol-capable and cannot be mechanically comminuted within the reactor by movements of the material within a reasonable time frame, there would otherwise be the danger that the reactor would clog with these residues from the bottom and the process would come to a standstill. This can be counteracted by the discharge.
  • Oxidation residues when leaving the reduction zone are separated from coarse-particle oxidation residues by a moving mechanical separating device, and the coarse-particle ones Oxidation residues in the reduction zone are retained until sufficient process-related comminution.
  • the process can be operated particularly advantageously if the temperature in the oxidation zone is preferably 800-1400 degrees Celsius and particularly preferably 1000-1300 degrees Celsius.
  • the method can advantageously be operated by using wood chips and / or compacted wood pellets and / or pre-shredded waste wood as solid biomass particles.
  • the method can also be used
  • Olive kernels, palm kernel shells or with coconut shells can be realized as solid biomass particles.
  • plastic-containing solids or flammable organic liquids as synthetic carbon-rich substances. It can be advantageous if the plastic-containing solids, which can consist, for example, of plastic-containing waste fractions, are compacted before use in the DC reactor.
  • plastic-containing solids can be fed to the DC reactor together with the solid biomass particles or a separate material flow.
  • flammable organic liquids are to be used in liquid form
  • an advantageous embodiment is that these liquids are fed to the direct current reactor via the drying zone or via the pyrolysis zone.
  • One of the essential embodiments of the method according to the invention provides that the synthetic carbon-rich substances used have a higher calorific value than the solid biomass particles, so that the calorific value of the resultant
  • Synthesis gas is higher than that without the addition of synthetic
  • Hydrogen bromide or hydrocyanic acid can be bound as salts. At the same time, so can an adsorption of heavy metals on the basic substances can be used to advantage.
  • the basic substances are oxides or hydroxides or carbonates which have alkali or alkaline earth metals as cations.
  • the basic substances are oxides or hydroxides or carbonates which have alkali or alkaline earth metals as cations.
  • calcium oxide or calcium hydroxide or calcium carbonate are especially when using calcium oxide or calcium hydroxide or calcium carbonate.
  • the grain size of the basic substances is preferably selected in accordance with the particle size of the oxidation residues so that the basic substances are aerosol-capable and / or can be discharged via the discharge device at the bottom of the reactor. If discharge on the floor is not possible, the basic substances must also be in a suitable dust form in order to be discharged via the gas stream.
  • a mixture of different grain sizes of the basic substances can also be used accordingly.
  • the use of coarser grain sizes of the basic substances can be particularly useful if certain types of ash, which can arise from the oxidation of synthetic substances, will melt.
  • the melted ash residues can be bound by the coarser grains of basic material and over the
  • Discharge device are discharged at the bottom of the reactor, so that it can be effectively prevented that melted ash hinders the process in the reactor or brings it to a standstill.
  • Comminution processes are subject to, provided that they remain in the reactor.
  • the dust-containing synthesis gas is cooled and the fine-particle oxidation residues are separated from the synthesis gas using mechanical separation methods.
  • the separated, finely divided oxidation residues are at least partially post-oxidized in a downstream screw reactor and the resulting oxidizing gas is at least partially returned to the DC reactor and / or at least partially mixed with the synthesis gas generated.
  • the utilization of the synthesis gas generated can be advantageously designed by using the synthesis gas extraction device as a self-priming internal combustion engine is designed in which the synthesis gas serves as a fuel for generating mechanical energy and heat.
  • the synthesis gas is used as fuel in a gas turbine for generating mechanical energy and heat, and / or for driving heat engines that work with internal secondary media, by indirectly supplying its combustion heat.
  • the change in the calorific value of the synthesis gas caused by the admixture of synthetic carbon-rich substances requires special control measures in the particularly preferred variant of using a self-priming internal combustion engine and converting the mechanical energy into electrical current in order to operate the method according to the invention in a stable manner. It is preferred to keep the speed of the self-priming internal combustion engine constant in the preferred range by increasing or throttling the amount of synthetic gas drawn in and / or by regulating the counter-torque of the generator via the amount of electricity removed and / or by connecting or disconnecting individual ones from several mechanically coupled generators to keep.
  • the synthesis gas can be used in thermal processes as a replacement for fossil fuels or as a raw material for chemical processes. In this case it can be advantageous that the
  • Synthesis gas extraction device as a gas delivery unit, e.g. as a gas blower
  • synthesis gas is fed to the downstream utilization process.
  • Figure 1 shows a schematic representation of a solid biomass particles
  • the DC reactor 1 has different reaction zones in a vertical shaft. These are arranged from top to bottom as follows: drying zone 2, pyrolysis zone 3, oxidation stone 4 and reduction zone 5.
  • the solid biomass particles 6, for example wood chips, flow through these reaction zones from top to bottom and are in the oxidation zone 4 by inflowing oxygen-containing gas 7, for example partially oxidized with air.
  • the sensible heat thus generated acts by transferring heat upwards into the pyrolysis zone 3 and weakened into the drying zone 2.
  • the biomass particles are heated to such an extent that they are cracked thermally to form pyrolytically produced fission products.
  • gaseous fission products are produced, which are referred to as pyrolysis gas, and solid products
  • pyrolysis coke carbon-rich fission products
  • the remaining heat from the pyrolysis zone 3 acts by heat transfer even further up into the drying zone 2, where the biomass particles, which usually still contain residual water, are pre-dried.
  • the pyrolytically produced gaseous and solid fission products flow in cocurrent from the pyrolysis zone 3 into the oxidation zone 4.
  • the fission products are at least partially oxidized by air 7, which is introduced via injection lances 8.
  • the resulting oxidation gas essentially contains carbon dioxide, carbon monoxide and water vapor.
  • the enthalpy of oxidation released during the oxidation provides the necessary energy for the method according to the invention and ensures that the process can be operated autothermally, that is to say without further supply of thermal energy.
  • Pyrolysis coke and ash continue to flow down into the reduction zone 5. There, at least in part, the pyrolysis coke is chemically reduced by
  • the DC reactor has a moving mechanical separation device 9. This separating device 9 is used to remove only finely divided oxidation residues,
  • the ash bunker has a gas outlet 11 A through which the synthesis gas flows out and at the same time at least partially discharges the fine-particle oxidation residues as an aerosol.
  • the ash bunker 10 has a discharge device 11B, via which those portions of the oxidation residues are discharged which do not have suitable physical properties, for example not a sufficiently small particle size for the formation of an aerosol.
  • the coarser oxidation residues are kept in the reduction zone 5 by the separating device 9 until their particle size has been reduced by the progressive reduction reaction to such an extent that they can flow through the separating device 9 to the ash bunker 10.
  • the fill level in the direct current reactor is automatically detected at regular intervals via a fill level measuring device 12, which is located in the head space 13 of the direct current reactor 1.
  • the fill level measuring device 12 When the fill level falls below a predetermined minimum, the fill level measuring device 12 generates a switch-on signal that initiates an automatic refilling with solid biomass particles 6 into the head space 13 with the aid of a biomass conveying device 14. Refilling is stopped by the level measuring device as soon as the level in the DC reactor reaches a predetermined maximum. This level control ensures that the level in the DC reactor is always automatically kept at a predetermined level.
  • the gas generating capacity of the DC reactor is controlled by a
  • Presetting synthesis gas extraction device 15 which draws a constant amount of gas from the DC reactor 1 via the gas outlet 11.
  • the gas vent leads to one
  • the synthesis gas produced in the DC reactor 1 and containing finely divided oxidation residues passes via the gas outlet 11 into a countercurrent heat exchanger 18, where the hot synthesis gas releases its sensible heat into the air 7.
  • Energy content of the synthesis gas is at least partially returned to the process via the injection lances 8 via the preheated air 7.
  • the synthesis gas cooled in the countercurrent heat exchanger 18 and containing finely divided oxidation residues is passed into a synthesis gas filter 19, where the finely divided oxidation residues are continuously separated from the synthesis gas.
  • the synthesis gas cleaned in this way passes through the filter gas outlet 20
  • the finely divided oxidation residues separated off in the synthesis gas filter 19 can also contain noteworthy portions of ash in pyrolysis coke.
  • the finely divided oxidation residues are discharged from the synthesis gas filter 19 at 21.
  • the fine-particle oxidation residues can be fed directly into suitable intermediate containers 22 or also directly into a suitable further use.
  • a preferred embodiment of the method according to the invention consists in that the finely divided and pyrolysis coke-containing oxidation residues are fed to a downstream post-reformer 23 after separation in the synthesis gas filter 19.
  • This post-reformer can preferably be a screw reactor.
  • Post-reformer the proportion of pyrolysis coke in the fine-particle oxidation residues is at least partially oxidized by supplying post-reforming air 24 to a mixture of carbon monoxide and carbon dioxide, which is taken as post-reforming gas from post-reformer 23 via a post-reforming gas filter 25.
  • the post-reforming air is fed via a post-reforming air blower 26 to the post-reformer 23 via the one metering unit 27.
  • this can be returned to the DC reactor 1 in order to convert the carbon dioxide content in the reduction zone 5 at least partially into carbon monoxide by reduction.
  • the return to the DC reactor 1 can advantageously take place at 28 in head space 13 and / or via injector lances 29 into oxidation zone 4.
  • the post-reforming gas can alternatively be 30 dem
  • Synthesis gas can be added for further use.
  • the ashes separated in the post-reforming gas filter 25 are conveyed via a discharge system 31 directly into suitable intermediate containers 22 and are disposed of.
  • the method according to the invention can be designed particularly advantageously if synthetic carbon-rich substances are used in the DC reactor 1 for the solid biomass particles.
  • This can be, for example, solid plastic-containing
  • Biomass particles are continuously admixed at 33 before entering the DC reactor.
  • the admixture can also take place via a separate lock system 34 directly into the head space 13 of the DC reactor 1.
  • the solid biomass particles offer the advantage during the gasification process that they remain dimensionally stable until reaching the oxidation zone 4 and thereby form a type of reaction migration bed for the synthetic carbon-rich substances 32. This effectively prevents lumps, for example when plastics are melted, and at the same time ensures sufficient gap volume for good gas permeability and gas distribution.
  • the synthetic carbon-rich substances migrate through the reaction zones of the DC reactor 1 parallel to the solid biomass particles and show a similar chemical behavior during the conversion into synthesis gas and fine particles
  • the admixture of high-calorific synthetic carbon-rich substances 32 in the DC reactor 1 effectively suppresses the gasification of the solid biomass particles 6, so that there is an equilibrium depending on the metering rate of the high-calorific synthetic carbon-rich substances 32 between used solid biomass particles 6 and the metered synthetic carbon-rich substances 32.
  • the method according to the invention is also suitable for the admixture of liquid synthetic carbon-rich substances 35.
  • This can be, for example, organic liquids or melts made of thermoplastic waste.
  • a preferred embodiment of the method according to the invention is that it flows directly into the head space 13 of the
  • DC gasifier 1 can be metered in via lances or nozzle systems at 36.
  • the admixture can also take place via lance systems at 37 in the drying zone 2 and / or at 38 in the pyrolysis zone 3 and / or at 39 in the oxidation zone 4.
  • halogen-containing plastic fractions for example halogen-containing plastic fractions is carried out.
  • Waste fractions can contain, for example, portions of polyvinyl chloride or flame retardants containing bromine.
  • the halogens are
  • Hydrogen chloride and / or as hydrogen bromide. It is acidic
  • Fission products which together with oxygen can potentially form toxic dioxins and furans in oxidation zone 4. Furthermore, such components are very corrosive, especially at high temperatures, and can cause enormous damage to them
  • the method according to the invention provides for the parallel admixture of basic substances 40, for example calcium oxide and / or calcium hydroxide.
  • Biomass particles are made at 41. Mixing in is particularly advantageous Dosing flow of the solid synthetic carbon-rich substances at 42 and or the admixture to the liquid synthetic carbon-rich substances at 43.
  • the basic substances can also be metered into the direct current reactor in a separate material flow via a lock system 44 in head space 13 of the direct current reactor 1.
  • the basic substances react spontaneously with the acidic cleavage products hydrogen chloride and / or hydrogen bromide to form calcium chloride or calcium bromide.
  • hydrogen chloride and / or hydrogen bromide react spontaneously with the acidic cleavage products hydrogen chloride and / or hydrogen bromide to form calcium chloride or calcium bromide.
  • Oxidation residues go through the process and are removed from the process either directly at 21 or after going through the still reformer process at 31.
  • the process according to the invention also permits the use of halogen-containing waste fractions without the formation of toxic dioxins and furans, or high-temperature corrosion leading to damage to system parts.
  • the invention is not limited to one of the above-described embodiments, but can be modified in many ways.

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

Abstract

L'invention concerne un procédé pour l'oxydation partielle de produits de dégradation générés par pyrolyse pour produire un gaz de synthèse (17) dans un réacteur à courant continu (1) traversé par des particules de biomasse solides (6), des substances synthétiques riches en carbone (32/35) étant mélangées avec les particules de biomasse solides (6), les particules de biomasse solides (6) étant utilisées dans une zone de séchage (2) et dans une zone de pyrolyse (3) ultérieure sous forme de surface réactionnelle migratoire destinée à la dégradation par pyrolyse des substances synthétiques riches en carbone (32/35), et l'oxygène lié chimiquement dans les particules de biomasse solides (6) servant au moins partiellement d'agent d'oxydation destiné à l'oxydation partielle, une introduction supplémentaire d'un gaz contenant de l'oxygène (7) dans une zone d'oxydation (4) ayant lieu, ce qui permet de convertir les particules de biomasse (6) au moins partiellement en résidus d'oxydation à fines particules dotées d'une taille moyenne de particule inférieure à 1 mm.
PCT/EP2019/074408 2018-09-17 2019-09-12 Procédé pour l'oxydation partielle de produits de dégradation générés par pyrolyse pour produire un gaz de synthèse dans un réacteur à courant continu Ceased WO2020058093A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN201980060770.6A CN112703245A (zh) 2018-09-17 2019-09-12 用于在顺流反应器中部分氧化热解产生的裂解产物以制备合成气体的方法
EP19770016.4A EP3853326A1 (fr) 2018-09-17 2019-09-12 Procédé pour l'oxydation partielle de produits de dégradation générés par pyrolyse pour produire un gaz de synthèse dans un réacteur à courant continu

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102018122727.2 2018-09-17
DE102018122727.2A DE102018122727A1 (de) 2018-09-17 2018-09-17 Verfahren zur Partialoxidation von pyrolytisch erzeugten Spaltprodukten zur Herstellung von Synthesegas in einem mit festen Biomasse-Partikeln durchströmten Gleichstromreaktor

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WO2020058093A1 true WO2020058093A1 (fr) 2020-03-26

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PCT/EP2019/074408 Ceased WO2020058093A1 (fr) 2018-09-17 2019-09-12 Procédé pour l'oxydation partielle de produits de dégradation générés par pyrolyse pour produire un gaz de synthèse dans un réacteur à courant continu

Country Status (4)

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EP (1) EP3853326A1 (fr)
CN (1) CN112703245A (fr)
DE (1) DE102018122727A1 (fr)
WO (1) WO2020058093A1 (fr)

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DE3633212A1 (de) 1986-09-30 1988-04-14 Kwu Umwelttechnik Gmbh Pyrolyseanlage
EP1436364A2 (fr) 2001-05-31 2004-07-14 Bernd Joos Dispositif de production d'un melange gazeux combustible
DE102007062414B4 (de) 2007-12-20 2009-12-24 Ecoloop Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
US20110094159A1 (en) * 2007-12-20 2011-04-28 Moeller Roland Method and Device for Reprocessing CO2 Containing Exhaust Gases

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