WO2024047624A1 - Réacteur à gaz de synthèse avec préchauffage pour alimentation en eau séparée et procédé pour celui-ci - Google Patents

Réacteur à gaz de synthèse avec préchauffage pour alimentation en eau séparée et procédé pour celui-ci Download PDF

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Publication number
WO2024047624A1
WO2024047624A1 PCT/IL2023/050860 IL2023050860W WO2024047624A1 WO 2024047624 A1 WO2024047624 A1 WO 2024047624A1 IL 2023050860 W IL2023050860 W IL 2023050860W WO 2024047624 A1 WO2024047624 A1 WO 2024047624A1
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WO
WIPO (PCT)
Prior art keywords
steam
reactor
feedstock
gas
synthesis
Prior art date
Application number
PCT/IL2023/050860
Other languages
English (en)
Inventor
Michael Zettner
Chanan GABAY
Tsachi SHOHAT
Uzi SEGAL
Original Assignee
Zohar Clean Tech. Ltd.
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Publication date
Application filed by Zohar Clean Tech. Ltd. filed Critical Zohar Clean Tech. Ltd.
Publication of WO2024047624A1 publication Critical patent/WO2024047624A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • 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
    • C10J3/04—Cyclic processes, e.g. alternate blast and run
    • 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
    • C10J3/14—Continuous processes using gaseous 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • 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
    • C10J3/30—Fuel charging devices
    • 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
    • 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
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • 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
    • C10J2300/1253—Heating the gasifier by injecting hot 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1693—Integration of gasification processes with another plant or parts within the plant with storage facilities for intermediate, feed and/or product
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/183—Non-continuous or semi-continuous 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
    • C10J2300/1853—Steam reforming, i.e. injection of steam only

Definitions

  • the invention is generally in the field of reactors that perform chemical conversions of fed organic materials to synthesis-gas based on heating the fed organic material, thus adding energy from outside to the performed chemi cal -reach on, to a temperature that the fed material reacts with water to generate synthesis-gas, which is a combustible gas-mixture, usually with relatively low energy-content, mainly consisting of carbon-monoxide, methane, some smaller hydrocarbon molecules, hydrogen, and residues of the reaction and the feedstock.
  • reactors are generally referred to as: shift-gas-reactors, pyrolysis-reactors, hydrolysisreactors, bio-gas-reactors, sump-gas-reactors, and various other names.
  • the invention here is a type of such synthesis-gas reactors with additional features for dividing the reaction into two main steps to enable more control of the reaction, to the end to save energy and improve and control the energy-content and homogeneity of the generated synthesis-gas.
  • Synthesis-gas reactors are known under many different names, which also change and changed over the many years, in which such reactors are used, and also with the purpose of such reactors. What they have all in common is firstly: these reactors need added thermal energy which is required to break up at least a large part of the molecules of the feedstock, thus enabling the desired chemi cal -reach on, and secondly: the kind of reductive chemi cal -reach on of the carbon-molecules of the broken-up molecules of the feedstock with the hydrogen, which is usually provided for the chemicalreaction in form of water, which is either at least partly in the feedstock or at least partly added to the feedstock.
  • the generated synthesis-gas of such a chemical-reaction contains compounds, which can be used as fuel, as they are combustible.
  • the generated synthesis-gas has a relatively low energy -content, compared to other fuels and or combustible compounds.
  • the generated synthesis-gas can vary in its composition, thus a fluctuation of the energy-content over time can occur.
  • the chemical-reaction in the synthesis-gas-reactor requires thermal-energy that is added to the chemi cal -reaction, as it is not provided by the chemi cal -reaction itself - as this would be the case in a combustion-reaction. This thermal energy is added from outside by heating elements.
  • the feedstock of a synthesis-gas-reactor can be from case to case completely different, depending on many reasons, one would just be: for which purpose the synthesis-gas-reactor is used.
  • the water content of the feedstock can be completely different from case to case. In case of dry wood as feedstock, the water content would be around 30%, while with wood that had not been dried, the water content would be around 70%.
  • the synthesis-gas reactor usually the largest part or at least a significant part of the energy, which is added to the synthesis-gas-reactor from outside, is used in the synthesis-gas reactor to first evaporate the water in the feedstock, or the water that had to be added, thus to change water from its liquid form to its gaseous form, before it can take part in the chemical reactions in the synthesis-gas- reactor.
  • the feedstock When the feedstock enters the synthesis-gas-reactor, then the feedstock is at a temperature level, which is too low to start the desired chemi cal -reaction.
  • the mass of the feedstock receives thermal energy and the temperature of the feedstock inside the synthesis-gas-reactor rises.
  • the temperature of the feedstock reaches the temperature, which is needed to evaporate water, usually around 100°C (212°F)
  • the added thermal energy is first consumed for the evaporation of the water-content of the feedstock, until almost all of the water is evaporated, before the temperature of the feedstock continues to rise further, beyond the temperature of around 100°C (212°F).
  • the evaporation of the water-content of the feedstock needs a specific amount of energy per kilogram of water, referred to as evaporation-enthalpy, as the heating of all other compounds also needs a specific amount of energy per kilogram of that compound.
  • the specific amount of thermal energy that is required to evaporate water is much higher than the specific amount of thermal energy that is required to heat other materials.
  • the time that is needed in a synthesis-gas-reactor to evaporate the water content of the feedstock or the added water is significantly more, than time needed to heat other compounds of the feedstock in the synthesis-gas-reactor.
  • the size of such a synthesis-gas-reactor significantly depends on the time it takes inside the synthesis-gas-reactor to evaporate the water content or the added water before a higher temperature of the feedstock can be reached.
  • the separated and extracted steam and vapour is sucked out of the preheated feedstock, before the remaining parts of the preheated feedstock enter the synthesis-gas-reactor, thus directly where the preheating step has reached or passed the temperature required for the evaporation of the water content of the feedstock.
  • the sucked-out steam and vapour is fed as steam and vapour, with a temperature above the evaporation-temperature, into a holding tank, parallel to the synthesi s-gas-reactor.
  • the sucked-out steam and vapour is then fed still as steam and vapour, at a temperature above the evaporation-temperature with a pressure above the ambient pressure inside the synthesis-gas-reactor and a heat-exchanger for a final heat boost into the synthesis- gas-reactor.
  • the said heat exchanger delivers the heat for the steam and vapour for additional raise of its temperature to a very high value.
  • the heating energy can be sourced from a heating element or by recovering heat from hot gases that come out at the end of the process and needs to be cooled down.
  • This feeding of the hot steam and vapour into the synthesis-gas-reactor is done in a controlled way by a compressor or pump.
  • This separating of the synthesis-gas-generation into two partial process-steps allows controlling the ratio between on one side the partially dried feedstock that entered the synthesis-gas-reactor after the steam and vapour had been separated and the water in form of the separated and extracted steam and vapour from the holding tank.
  • the chemical reaction between the organic compounds in the feedstock and the required water can be kept optimal concerning the ratio of the compounds containing the carbon- compounds and the compounds containing the necessary hydrogen.
  • the generated synthesis-gas is more homogeneous, even in case of an inhomogeneous feedstock.
  • the synthesis-gas-reactor does not have to perform the necessary heating and converting liquid water into steam, which significantly shortens the time required for the process of converting organic compounds into synthesis-gas and thus allows either increasing the capacity of feedstock per time, or keeping the reactor smaller, without changing the outputquantity of synthesis-gas.
  • the preheating-step with the task to reach the evaporation-temperature for water operates at a much lower temperature-level, than the chemical reaction to convert organic compounds into synthesis-gas, the preheating step for evaporating water can be realised with simpler means and thus with lower costs, than the synthesis-gas-reactor, where much higher temperatures are required.
  • the invention here shows a way how to use the separated steam and vapour by means of aimed injections at certain specific locations within the synthesis-gas-reactor to induce a stable vortex, increase the mixing of the compounds in the synthesis-gas-reactor and thus increase the efficiency of the chemical reaction, respectively decrease the quantity of compounds that did not completely react thus increase the yield of combustible synthesis-gas, decrease the time required for the different molecules to react, and thus increase overall yield of combustible gases, efficiency, and controllability of such synthesis-gas-reactors.
  • the invention pertains to a reactor system for the generation of a combustible gas-mixture of carbon-monoxide, methane, carbon-dioxide, hydrogen, water, and other compounds from a provided feedstock of compounds containing carbon and water
  • said reactor system comprising: a closed reactor; means of feeding said feedstock through at least one designated opening into said closed reactor; heating means for heating said compounds inside said closed reactor from outside said closed reactor; at least one suction means; at least one holding tank; at least one other means for receiving or taking and injecting and additional heating of generated steam and other generated vapours from said holding tank, wherein said heating means is configured for heating said feedstock in at least one preheating step that precedes opening said closed reactor for feeding said feedstock to a temperature that evaporates water contained in said feedstock, wherein said heating of said compounds inside said closed reactor from outside is made to a temperature that starts a reaction and generates said gas-mixture, said at least one suction means is configured to suck generated steam and
  • Fig. 1 is a schematic presentation of the complete system in a most simplified form. Detailed Description of the Drawings
  • Fig- 1 is a schematic presentation of the complete system in a most simplified form.
  • the inlet (1) At the top of the schematic presentation is the inlet (1).
  • the arrow points to the direction, to which the feedstock is proceeding.
  • the additional preheating step (2) is following directly.
  • the heating is indicated on the left side of said preheating step with arrows with the number (6).
  • the feedstock is proceeding, after the extraction of the steam and vapour (2), to the inlet of the synthesis-gas-reactor (3) and enters the closed inner space of the synthesis-gas-reactor (4).
  • the synthesis-gas-reactor is defined by its outer confinement (5).
  • the heating of the synthesis-gas-reactor is just generally indicated by the arrows from the left side (6). In reality, the heating is on all sides to ensure good or optimal transfer and distribution of thermal energy into the synthesis-gas-reactor and thus the feedstock.
  • the synthesis-gas that is generated in the synthesis-gas-reactor is leaving the reactor in this schematic presentation at the top left side (7).
  • centrifugal-absorber (8) indicated at the top of the reactor on the right side, at the point where the extracted steam and vapour are sucked from the preheating step (2) by the compressor, pump or blower (9).
  • An additional heater or heat-exchanger (12) is shown in the duct from the holding-tank to the synthesis-gas-reactor.
  • three inlets for the steam and vapour at the side (13) and one injection point (14) from the bottom that may be used to generate turbulences and stable vortexes or other fluid-mechanical effects to further increase mixing of feedstock with steam inside the synthesis-gas-reactor (4).
  • synthesis-gas is generated by heating-up compounds, which contain carbon and let them react at high temperature with compounds, like water, which contain hydrogen that is required for the chemical reaction that generates a carbon-hydrogen-gas-mixture.
  • This gas mixture contains as main components: carbon-monoxide, methane, carbon-dioxide, hydrogen, steam, and then: many kinds of carbon-hydrogen compounds and the residues from the chemi cal -reach on.
  • These gas mixtures are referred to in many different ways: sump-gas, water- gas, bio-gas, etc.
  • the term synthesis-gas is very generally used and thus will also be here the used term for those kinds of gas mixtures.
  • the invention here can be used for all those kinds of synthesis-gas-reactors, independent from the type of feedstock, the size and whether the specific synthesis-gas-reactor has been modified or optimised for certain processes or a specific feedstock.
  • the invention can also be used independent from the kind or types of heating for the synthesis-gas-reactor, from electrical heaters to gas-fired burners, to plasma-torches, used to increase the temperature inside the synthesi s-gas-reactor.
  • the feedstock of a synthesis-gas-reactor is heated inside the synthesis-gas-reactor to a temperature that starts breaking molecular-bonds in the molecules of the compounds of the feedstock which enables the chemical reaction to start.
  • the feedstock is also heated as in any conventional synthesis-gas-reactor, however in an additional preceding first step, before the feedstock enters the synthesis-gas- reactor, and only to a temperature that leads to at least a significant evaporation of water.
  • the feedstock at this additional preceding first step would be heated at atmospheric pressure to a temperature of 100°C to 120°C, thus reaching in nearly all of the feedstock a temperature, which leads to the evaporation of the water, contained in the feedstock.
  • Heating to a temperature that is at or above the evaporation-temperature of water is reached in any possible way, as it is the case today with synthesis-gas-reactors.
  • a possible way would be to add some heating-sleeves at the feeding-system or feeding-duct, before the feedstock enters the synthesis-gas-reactor.
  • the opening of the synthesis-gas-reactor, where the feedstock enters, has a limited cross-section, it cannot be unlimited.
  • a step is required for preparing, shredding, dosing, or otherwise enabling the feedstock to enter the synthesis-gas-reactor through its opening.
  • Some kind of closed duct from this preparation-step to the entrance-opening of the synthesis-gas-reactor would be the best place for the preheating-step.
  • the preheating step could also be located before such a preparation-step.
  • the evaporated water forms steam as the gaseous form of the water and is referred to hereinafter as steam.
  • vapour or vapours Other compounds that also evaporate are referred to hereinafter without further specification as vapour or vapours.
  • the energy that is required to heat the feedstock to and above the evaporation temperature of the water and the energy that is required to evaporate at least a significant amount of the water in the feedstock is added from outside. The same amount of energy would be necessary for heating and thus the evaporation of water if it were without this preheating-step in the conventional way inside the synthesis-gas-reactor.
  • the pre-heating-step is for the overall energy-balance of the complete system neutral. No additional energy for heating has to be provided for the synthesis-gas-reactor-system, with this new invention.
  • an additional absorber for example a centrifugal-absorber, or a filter might be needed, if the feedstock contains dust-like particles or liquids that form mist and droplets. Even if some dust or solid or liquid compounds in small percentage would go with the suction into the separated steam and vapour, the overall function and or functionality of the complete system would not be changed or minimised.
  • the additional absorber or filter could be used in cases, where for example fine sand or other solids in fine form would be sucked in and end up in the holding-tank for steam and vapour, where those fine solids could separate by gravity and built up layers on the bottom of the holding-tank for steam and vapour.
  • the extracted steam and vapour is fed with the same compressor, blower, or pump into a holding tank.
  • the holding-tank functions as a buffer for the steam and vapour.
  • some water in form of either steam or liquid water can be added from outside - for example in form of regular tap-water - to the holding tank.
  • this added water is in form of steam or liquid water is for the process less relevant, as there is also an optional additional heater for the steam that follows in the process the holdingtank, as described further below [ in Figure 1 this is shown as 12 ].
  • the extracted steam and with it some vapours of other compounds, with a lower evaporation temperature, than water, which might have been in the feedstock, are buffered in the holdingtank. It is possible if for example a set maximum-level is reached to remove some of the steam in case it will not be needed for the reaction. This can be the case if the feedstock contains a large percentage of water, more than needed for the designed and desired chemi cal -reach on in the synthesi s-gas-reactor.
  • vapours which are lighter, than steam by the specific density of those compounds By just using an outlet from the bottom of the holding tank it would be possible to separate vapours which are lighter, than steam by the specific density of those compounds and leave them in the holding-tank to be transferred into the synthesis-gas-reactor.
  • the holding tank provides the means for controlling the reaction in the synthesis-gas- reactor, independent from the composition of the feedstock.
  • the holding-tank is the reservoir or the steam-injection into the synthesis-gas-reactor.
  • the chemical reaction can be kept at all times at an optimum and as a direct consequence also the generated synthesis-gas would be without fluctuations in its composition, or just minor fluctuations in its composition.
  • a conventional synthesis-gas-reactor has no or at best a very limited possibility of mixing the compounds for the chemical reaction.
  • the steam would then, additionally to the heating of the synthesis-gas-reactor from outside, also heat the compounds inside the synthesis-gas-reactor.
  • a smaller size of the synthesis-gas-reactor for the same yield leads to smaller total heatlosses, as the surfaces of a smaller reactor are smaller than for a larger reactor with the same yield.
  • a homogeneous reaction in the synthesis-gas-reactor with the described invention leads also to a constant quality of the generated synthesis-gas, what is also a commercial advantage as such a homogeneous synthesis-gas can be used more easily and for more purposes.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un réacteur de synthèse de gaz qui effectue des conversions chimiques de matières organiques alimentées en gaz de synthèse sur la base du chauffage de la matière organique alimentée, ajoutant ainsi de l'énergie depuis l'extérieur à la réaction chimique effectuée, à une température telle que la matière alimentée réagit avec l'eau pour générer un gaz de synthèse, qui est un mélange de gaz combustible, généralement avec une teneur en énergie relativement faible, principalement constitué de monoxyde de carbone, de méthane, de certaines molécules d'hydrocarbone plus petites, d'hydrogène et de résidus de la réaction et de la charge d'alimentation. Les réacteurs comportant des caractéristiques supplémentaires divisent la réaction en deux étapes principales pour permettre une plus grande maîtrise de la réaction afin d'économiser de l'énergie et améliorer et contrôler la teneur en énergie et l'homogénéité du gaz de synthèse généré.
PCT/IL2023/050860 2022-08-31 2023-08-15 Réacteur à gaz de synthèse avec préchauffage pour alimentation en eau séparée et procédé pour celui-ci WO2024047624A1 (fr)

Applications Claiming Priority (2)

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US202263402660P 2022-08-31 2022-08-31
US63/402,660 2022-08-31

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WO2024047624A1 true WO2024047624A1 (fr) 2024-03-07

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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090239279A1 (en) * 2007-05-11 2009-09-24 The Texas A & M University System Integrated Biofuel Production System

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090239279A1 (en) * 2007-05-11 2009-09-24 The Texas A & M University System Integrated Biofuel Production System

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