WO2017186482A1 - Procédé et dispositif de production de gaz de synthèse - Google Patents

Procédé et dispositif de production de gaz de synthèse Download PDF

Info

Publication number
WO2017186482A1
WO2017186482A1 PCT/EP2017/058670 EP2017058670W WO2017186482A1 WO 2017186482 A1 WO2017186482 A1 WO 2017186482A1 EP 2017058670 W EP2017058670 W EP 2017058670W WO 2017186482 A1 WO2017186482 A1 WO 2017186482A1
Authority
WO
WIPO (PCT)
Prior art keywords
converter
hydrogen
carbon
splitting
hydrocarbon
Prior art date
Application number
PCT/EP2017/058670
Other languages
German (de)
English (en)
Inventor
Olaf Kuehl
Mark MISSELHORN
Original Assignee
CCP Technology GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE102016005188.4A external-priority patent/DE102016005188A1/de
Application filed by CCP Technology GmbH filed Critical CCP Technology GmbH
Publication of WO2017186482A1 publication Critical patent/WO2017186482A1/fr

Links

Classifications

    • 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
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/026—Increasing the carbon monoxide content, e.g. reverse water-gas shift [RWGS]
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/06—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by mixing with gases

Definitions

  • the present application relates to a method and an apparatus for producing synthesis gas with variable H2 / CO ratio.
  • the object of the present invention is therefore to provide a method and an apparatus for producing synthesis gas with a variable H 2 / CO ratio.
  • This object is achieved by a method for the production of synthesis gas, comprising the following steps: splitting a hydrocarbon fluid, in particular a first gas having the composition C n H m , into carbon and hydrogen in a reaction space of a hydrocarbon converter with the introduction of heat the carbon and the hydrogen after the decomposition have a temperature of at least 800 ° C; Passing the carbon and hydrogen recovered from the decomposition into a reaction space of a C0 2 converter; Mixing C0 2 from an external source with the carbon and hydrogen in the CO 2 converter; Converting the C0 2 and the carbon obtained by the resolution into CO at a temperature of 800 to 1700 ° C, so that a first synthesis gas mixture is formed; Mixing the first synthesis gas mixture with additional hydrogen, so that a second synthesis gas mixture is produced, which has a higher hydrogen content than the first synthesis gas mixture.
  • the additional hydrogen is generated by the following steps: conduct a second gas having the composition C n H m in a reaction space of a solids converter containing a solid bed of carbonaceous granules, in particular a moving bed guided through the reaction space, wherein the solid bed at least locally has a temperature of 800 to 1700 ° C; Splitting the second gas having the composition C n H m into carbon and hydrogen which forms the additional hydrogen; Separating the carbon obtained by the decomposition and the additional hydrogen by depositing the carbon on the carbonaceous granules.
  • the additional hydrogen is thus added to the first synthesis gas mixture and makes it possible to variably control the H 2 / CO ratio of the finally resulting second synthesis gas mixture and to adapt it to subsequent processes. If not all of the available hydrogen is needed to control the H 2 / CO ratio, the remaining hydrogen can be sold.
  • the supply of heat for splitting the hydrocarbon fluid (the first gas having the composition C n H m ) in the hydrocarbon converter takes place primarily via a plasma.
  • This is a particularly direct and thus efficient form of energy input and allows a continuous splitting of a stream of hydrocarbons.
  • the hydrocarbon fluid is thereby split into a mixture of carbon (C particles) and hydrogen (H 2 ), also referred to as H 2 / C aerosol.
  • the cleavage is carried out in a Kvaerner reactor.
  • the splitting of the hydrocarbon fluid and the conversion of the C0 2 and the carbon are carried out in CO without catalyst. This avoids costs as catalysts are expensive. Furthermore, a trouble-free process with a long running time is made possible, since no catalysts have to be replaced or cleaned.
  • the energy required to reach the temperature of 800 to 1700 ° C for the C0 2 conversion in the C0 2 converter derives essentially completely from the heat provided for the decomposition of the hydrocarbon fluid. Essentially, this means that at least 80%, especially at least 90% of the heat required is from the splitting step. As a result, the introduced energy is optimally utilized.
  • the CO 2 is provided from an external source, for example, exhaust gas of an internal combustion engine or blast furnace gas, which is generated by reduction of a metal ore in a blast furnace shaft and contains CO 2 . Since carbon attaches to the granules in the solid converter, the granules can be used after removal from the solids converter in a blast furnace shaft for metal production. Therefore, there is a particular advantage when the method is used in the vicinity of a metallurgical plant and the CO 2 is used, which is produced in the blast furnace shaft by reduction of metal oxide or in incineration plants. The carbon-enriched granules from the solids converter are considered to be a valuable raw material for metal production.
  • an external source for example, exhaust gas of an internal combustion engine or blast furnace gas, which is generated by reduction of a metal ore in a blast furnace shaft and contains CO 2 . Since carbon attaches to the granules in the solid converter, the granules can be used after removal from the solids converter in a blast furnace shaft for metal production
  • the carbon of the granulate does not change to CO upon contact with H 2 O, the granules in the solids converter are not brought into contact with H 2 O or water vapor. If not all of the available hydrogen is needed to control the H 2 / CO ratio, the remaining hydrogen can be used as the reductant in the blast furnace shaft. Similarly, unneeded CO of the first synthesis gas mixture can be used as a reductant in the blast furnace shaft.
  • a carbonaceous granulate is here to be understood as meaning a material which advantageously consists of solid grains which contain at least 50% by weight, in particular at least 80% by weight, more preferably at least 90% by weight of carbon.
  • the carbonaceous granules preferably have a grain size (equivalent diameter), which can be determined by sieving with a certain mesh size, from 0.5 to 100 mm, in particular from 1 to 80 mm.
  • the carbonaceous granules may be spherical. In the method described here, a multiplicity of different carbonaceous granules can be used, for example from coal, coke, coke breeze and / or mixtures thereof. Coke breeze usually has a grain size of less than 20 mm.
  • the carbonaceous granules 0 to 15 wt .-% based on the total mass of the granules, preferably 0 to 5 wt .-%, metal, metal oxide and / or ceramic.
  • the carbonaceous granules are upgraded for use in a blast furnace shaft in the method and apparatus described herein.
  • the energy required to produce the temperature of 800 to 1700 ° C. of the carbon-containing granular solids bed can be generated by thermal energy in the reaction space of the solids converter.
  • a partial oxidation / combustion of the carbonaceous granules can be used by means of injected air.
  • the required energy can be introduced via a hot gas from the outside into the reaction space of the solids converter.
  • the thermal energy required in the solids converter is produced by oxidation or partial oxidation of a fuel comprising hydrocarbons and / or hydrogen.
  • a fuel comprising hydrocarbons and / or hydrogen.
  • the oxidizing agent for example, air, oxygen-enriched air or pure oxygen is used. This oxidation may be carried out outside the reaction space, the resulting hot gas then being introduced into the reaction space and passed over the carbonaceous solid, giving off heat energy to the carbonaceous granules and / or the gases to be reacted.
  • the oxidizing agent may also be introduced into the reaction space where it is mixed with an existing fuel and reacted.
  • the carbonaceous granules have low-grade Kokereikoks on lignite, coal or biomass basis, can escape from the pyrolysis gases at elevated temperature, so a pyrolysis zone is provided.
  • oxygen or air is then fed in after the pyrolysis zone in order to at least partially oxidize the pyrolysis gases.
  • the thermal energy required in the solids converter is generated by an electrical heater in which a gas (in particular hydrogen) is heated by an electrical heating device (in particular a plasma torch) and is introduced into the reaction space.
  • an electrical heating device in particular a plasma torch
  • the solid bed of carbonaceous granules is preferably carried out as a moving bed continuously and in particular with the aid of gravity.
  • the carbonaceous granules with ambient temperature in a first conveying direction preferably in the direction of gravity from top to bottom
  • the second gas e.g., methane or natural gas
  • the second gas is passed through the solids bed of carbonaceous granules in a second conveying direction, counter to the first conveying direction, and split into carbon and "additional" hydrogen by the high temperature of the carbonaceous granules.
  • the additional hydrogen obtained by the splitting of the second gas is thus cooled by contact with the carbonaceous granules.
  • the reaction space of the solid converter is preferably designed as a vertical shaft, so that the movement of the moving bed can be achieved solely under the action of gravity.
  • a moving bed allows a continuous or quasi-continuous mode of operation and can be carried out homogeneous and uniform flow.
  • an apparatus for producing synthesis gas comprising: a hydrocarbon converter for splitting a hydrocarbon fluid into carbon and hydrogen, the hydrocarbon converter having at least one process cavity with at least one inlet for a hydrocarbon fluid at least one output for carbon and hydrogen and at least one unit for introducing energy into the process space; a C0 2 converter for converting C0 2 into CO, wherein the CO 2 converter at least one further process space with at least one input for CO 2 for Introducing CO 2 from an external source into the CO 2 converter, having at least one input for carbon and hydrogen and at least one output for synthesis gas (first synthesis gas mixture), the input for carbon and hydrogen communicating directly with the at least one output of the hydrogen converter is connected; a solids converter having a reaction space containing a solid bed of carbonaceous granules, in particular a moving bed guided through the reaction space, wherein the solids converter has an inlet for a second gas having the composition C n H m in the solid bed, further an inlet for carbonaceous Granules,
  • the solids converter further has an outlet for hydrogen; wherein the synthesis gas output of the C0 2 converter and the hydrogen outlet of the solids converter are connected to a mixing device and / or a CO converter.
  • This apparatus is provided for carrying out the method described above and allows additional hydrogen to be generated which can be added to the first synthesis gas mixture.
  • it is possible to variably control the H 2 / CO ratio of the resulting second synthesis gas mixture and to adapt it to subsequent processes.
  • the at least one unit for introducing energy into the process space of the hydrocarbon converter is advantageously designed such that it can generate temperatures at least locally above 1000 ° C.
  • it has a plasma unit, which allows a particularly direct and efficient form of energy input and a continuous splitting of a stream of hydrocarbons, through which a H 2 / C-aerosol is generated.
  • the cleavage is carried out in a Kvaerner reactor.
  • the external source of C0 2 is preferably formed by a combustion power plant or a blast furnace shaft, since this results in advantageous synergy effects, as described in more detail above.
  • a synthesis gas with any H 2 / CO ratio can be provided by means of the mixing device and sold, for example.
  • the CO converter preferably has one of the following: a Fischer-Tropsch converter, an SMDS converter, a Bergius-Pier converter, a pier converter or a combination of a pier Converter with a MtL converter. Since the H 2 / CO ratio of the second synthesis gas mixture can be adjusted very finely, these CO converters can work very efficiently. It is also considered a combination of a mixing device with a subsequent CO converter. The mixing device may also be part of the CO converter.
  • the solids converter and the hydrocarbon converter are separate devices, as also seen in the drawings.
  • the hydrocarbon converter and the CO 2 converter can be directly connected to each other, so that the lowest possible heat loss occurs between them. It is also possible that the hydrocarbon converter and the CO 2 converter merge into one another.
  • FIG. 1 shows an embodiment of the device described herein from the process of the method is clear.
  • Fig. 2 is a schematic representation of the solids converter.
  • Fig. 3 is a schematic representation of the hydrocarbon converter, the C0 2 converter and the CO converter, wherein on the left in Fig. 3, the supply line for additional hydrogen is indicated by the solids converter.
  • top, bottom, right and left as well as similar statements refer to the orientations and arrangements shown in the figures and are only used to describe the embodiments. These terms may indicate preferred arrangements, but are not to be construed in a limiting sense.
  • the wording "essentially” and similar formulations in relation to parallel, perpendicular or angular data shall include deviations of ⁇ 3 degrees and shall include deviations of 5% based on other data and quantities.
  • the following description also describes processes and devices that perform "hot” substances or “hot” processes. In the context of this description, the term “hot” is intended to describe a temperature above 300 ° C.
  • FIG. 1 shows schematically an apparatus for the production of synthesis gas. From Fig. 1, the basic procedure is clear. Figure 1 illustrates by arrows the flows of the various materials and materials, but the arrows do not represent precise locations of inlets into or outlets from the individual converters or plant components.
  • the apparatus 1 for the production of synthesis gas has a Feststoffkonver- ter 2 and a hydrocarbon converter 3 (see Fig. 1 and 3), which has a hydrocarbon inlet 4 for a hydrocarbon fluid and an outlet 5 for carbon and hydrogen.
  • the synthesis gas producing apparatus 1 further comprises a CO 2 converter 7 having a CO 2 input 8 for CO 2 from an external source, an input 9 for carbon and hydrogen, and an output 10 for synthesis gas.
  • the hydrocarbon converter 3 and the CO 2 converter 7 are arranged such that the output 5 of the hydrocarbon converter 3 is connected via a direct connection to the input 9 of the CO 2 converter 7, wherein the output 5 of the hydrocarbon converter 3 also directly 9 Input of the CO 2 converter 7 can form.
  • carbon and hydrogen from the hydrocarbon converter 3 can be transported directly into the C0 2 converter 7.
  • the hydrocarbon converter 3 is any hydrocarbon converter that can convert feed hydrocarbons to carbon and hydrogen.
  • the hydrocarbon converter 3 can be operated thermally or with a plasma.
  • a thermally operated hydrocarbon converter 3 a hydrocarbon fluid introduced into a reaction space is heated to a decomposition temperature by any heat source.
  • a plasma-operated hydrocarbon converter the energy is supplied via a plasma arc.
  • An introduced hydrocarbon fluid decomposes into carbon and hydrogen at the decomposition temperature.
  • the separation of the hydrocarbons should take place as far as possible in the absence of oxygen in order to prevent the undesired formation of carbon oxides or water.
  • small amounts of oxygen, which are introduced, for example, with the hydrocarbons are again not detrimental to the process.
  • the hydrocarbon converter 3 has a process space with a hydrocarbon fluid inlet 4, at least one unit 12 for introducing decomposition energy into the hydrocarbon fluid, and at least one outlet.
  • the splitting energy is at least partially provided by heat generated, for example, by a plasma (plasma reactor). However, it can also be made available in another way (thermal reactor). Primarily, a splitting occurs via heat.
  • the hydrocarbon fluid should be heated above 1000 ° C, especially at a temperature above 1500 ° C.
  • a plasma-operated hydrocarbon converter can be selected as the plasma gas any suitable gas which is supplied from the outside or produced in the hydrocarbon converter.
  • plasma gas for example inert gases are suitable, for example argon or nitrogen.
  • a plasma reactor is used as the hydrocarbon converter 3, which provides the required heat by means of a plasma arc in a plasma torch 12.
  • An advantageous embodiment of a plasma reactor is a Kvaerner reactor.
  • other plasma reactors are also known which operate at lower temperatures, in particular below 1000 ° C., and in addition to the heat introduce additional energy into the hydrocarbon, for example via a microwave plasma.
  • the invention contemplates both reactor types (and also those which operate without a plasma), in particular also in combination with one another.
  • Hydrocarbon converters which operate at a temperature in the process space of more than 1000 ° C. are referred to below as high-temperature reactors, while those which operate at temperatures below 1000 ° C., in particular at a temperature between 200 ° C. and 1000 ° C. , referred to as low-temperature reactors.
  • hydrogen and carbon are generated from hydrocarbons (C n H m ) by means of heat and / or a plasma.
  • the hydrocarbons are preferably introduced into the process space in gaseous form (first gas). In the case of hydrocarbons which are liquid under normal conditions, these can be gaseous form prior to introduction into the hydrocarbon converter 3, or they could also be introduced in finely atomized form.
  • the hydrocarbon fluid preferably consists of a stream of natural gas, methane, liquid gases or heavy oil, and preferably a stream of conventional or non-conventional natural gas, as well as liquid gases ("wet gases").
  • introduced hydrocarbon fluids are split at high temperature into a mixture of carbon (C particles) and hydrogen (H 2 ), also referred to as H 2 / C aerosol. This mixture of carbon particles and hydrogen remains separated even after cooling.
  • the CO 2 converter 7 may be any suitable CO 2 converter capable of producing carbon monoxide (CO) from carbon (C) and carbon dioxide (CO 2 ).
  • the CO 2 converter 7 operates according to a part of the known in the art blast furnace reaction, which takes place at temperatures between about 750 ° C and 1200 ° C without the need for a catalyst.
  • the CO 2 converter 7 operates at a temperature between 800 ° C and 1000 ° C, wherein the required for achieving this temperature heat is provided primarily by the material which comes out of the hydrocarbon converter 3, as explained in more detail below becomes.
  • CO 2 is passed over hot carbon or mixed with this (and possibly hydrogen) to be converted according to the chemical equation CO 2 + C - 2 CO.
  • the CO 2 converter 7 works best at the Boudouard equilibrium and a temperature of 1000 ° C. At temperatures of 800 ° C, about 94% carbon monoxide is supplied, and at temperatures around 1000 ° C, about 99% carbon monoxide is supplied. A further increase in temperature does not bring any significant changes.
  • a carbonaceous granulate for example coke breeze
  • the granules are then passed through reaction space R under the action of gravity in a moving bed W down.
  • a methane-containing second gas for example natural gas or methane
  • the second gas which has ambient temperature at its entry into the reaction space R, is heated on the way up in heat exchange with the granules (moving bed W).
  • the second gas is split into carbon and hydrogen, wherein the carbon deposits more than 95% of the grains of the carbonaceous granules.
  • the hydrogen formed in the splitting continues to flow against the conveying direction of the granules and finally emerges as "additional" hydrogen from the Solid state converter off.
  • the resulting hydrogen continues to flow upward, being cooled in heat exchange with the cooler granules of the moving bed W, so that the additional hydrogen can be withdrawn via a hydrogen outlet 17 at a temperature above the ambient temperature, but at least 500 K below the temperature at the splitting of the second gas, is located.
  • the additional hydrogen is passed to a mixing device 19 and mixed with the synthesis gas from the C0 2 converter 7 (first synthesis gas mixture) in order to achieve a desired mixing ratio of H 2 to CO in the finally produced second synthesis gas mixture.
  • a possibility for heating the granulate and moving bed is described.
  • a part of the hydrogen is separated, which is then heated in a likewise optional electric heater PH using an arc (plasma torch) to hot hydrogen gas.
  • the hot hydrogen gas is introduced into the high-temperature zone H, where it provides the energy required for the splitting of the second gas.
  • the granules are stripped off with deposited carbon.
  • the deposited carbon granules may be used, for example, as a coke additive or carburizing agent in foundries because of their high carbon content and low ash and sulfur content.
  • the remainder 23 of the deposited carbon granules may be sold as a blast furnace coke (ie, as a high quality product) or used directly in a blast furnace shaft 25 disposed adjacent to the syngas production device 1 described herein and as an external CO 2 source for the operation of the C0 2 converter 7 is used.
  • the second synthesis gas mixture is adjusted in the mixing device 19 to a desired H 2 / CO ratio, and it consists of the first synthesis gas mixture (from the C0 2 converter) and the additional hydrogen from the solids converter 2.
  • a fine adjustment of the H 2 / CO ratio and also the temperature of the first synthesis gas mixture can be effected by a lesser amount of C0 2 but in addition H 2 0 is added to the C0 2 converter 7.
  • Additional H 2 O may also be added at a location between the C0 2 converter 7 and the mixing device 19 as long as the residual temperature is sufficient to achieve conversion of hot C particles with H 2 O (C + H 2 O -> H 2 + CO).
  • the H 2 / CO ratio of the final generated second synthesis gas mixture will meet the requirements of a customer or a subsequent process step in a CO converter.
  • the synthesis gas production apparatus 1 further comprises an optional CO converter 27.
  • the CO converter 27 may be any CO converter for producing synthetic hydrocarbons (with or without a functional group).
  • the CO converter 27 is preferably a Fischer-Tropsch converter, an SMDS converter, a Bergius-Pier converter, a Pier converter or a combination of a Pier converter with a MtL converter with a corresponding catalyst and a temperature and / or pressure control unit.
  • a Bergius-Pier converter the Bergius-Pier process well known to those skilled in the art, in which hydrocarbons are produced by hydrogenating carbon with hydrogen in an exothermic chemical reaction, is used.
  • the range of starting materials from the Bergius-Pier process depends on the reaction conditions and the reaction procedure. There are mainly obtained liquid end products that can be used as fuels, for example Heavy and medium oils.
  • Known developments of the Bergius-Pier process are, for example, the Konsol process and the H-Coal process.
  • the CO converter 27 has a Fischer-Tropsch converter.
  • a Fischer-Tropsch converter catalytically converts a synthesis gas to hydrocarbons and water.
  • Fischer-Tropsch reactors and Fischer-Tropsch method are known, which should not be shown here in detail.
  • the main reaction equations are as follows:
  • the Fischer-Tropsch processes can be carried out as a high-temperature process or as a low-temperature process, the process temperatures generally being between 200 and 400.degree.
  • a Fischer-Tropsch converter typically produces a hydrocarbon compound from liquefied gases (propane, butane), gasoline, kerosene (diesel oil), soft paraffin, hard paraffin, methanol, methane, diesel fuel, or a mixture of several of them.
  • the Fischer-Tropsch synthesis is exothermic, as known to those skilled in the art.
  • the heat of reaction from the Fischer-Tropsch process can be used, for example, for preheating CO 2 by means of a heat exchanger (not shown in the figures). It is, for example, a two-stage preheating of the introduced into the CO 2 converter CO 2 contemplated by first preheating means of the heat from the CO converter 27 (converter in the embodiment as a Fischer-Tropsch) is carried out, and thereafter further heating of the CO 2 by means of heat from one or more heat exchangers (not shown).
  • waste heat generated during operation of a Fischer-Tropsch converter can be used to preheat air or oxygen and to dry ore or aggregates which are introduced and blown into the blast furnace shaft 25.
  • the hydrocarbon fluid to be split is, for example, natural gas, methane, liquefied petroleum gas, heavy oil or a mixture thereof.
  • the hydrocarbon fluid to be split is natural gas or methane (first gas of composition C n H m ), but the other hydrocarbon fluids can also be processed.
  • the second gas introduced into the solids converter is natural gas or methane (second gas).
  • the solids converter and the hydrocarbon converter are always separate devices.
  • the hydrocarbon converter and the C0 2 converter can be directly connected to each other, so that the lowest possible heat loss occurs between them. It is also possible that the hydrocarbon converter and the C0 2 converter merge into one another.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention concerne un procédé de production de gaz de synthèse avec un rapport H2/CO variable, qui comprend les étapes suivantes : fractionner un fluide contenant des hydrocarbures, en particulier un premier gaz ayant la composition CnHm, en carbone et en hydrogène dans une chambre de réaction d'un convertisseur d'hydrocarbures, sous apport de chaleur, le carbone et l'hydrogène présentant après fractionnement une température d'au moins 800°C; guider le carbone et l'hydrogène résultant du fractionnement dans une chambre de réaction d'un convertisseur de CO2; mélanger du CO2 provenant d'une source extérieure avec le carbone et l'hydrogène dans le convertisseur de CO2; convertir le CO2 et le carbone résultant du fractionnement en CO à une température de l'ordre de 800 à 1700°C, de sorte à obtenir un premier mélange de gaz de synthèse; mélanger le premier mélange de gaz de synthèse avec de l'hydrogène additionnel, de manière à obtenir un second mélange de gaz de synthèse qui contient une plus grande proportion d'hydrogène que le premier mélange de gaz de synthèse. L'hydrogène additionnel est obtenu selon les étapes suivantes : guider un second gaz ayant la composition CnHm dans une chambre de réaction d'un convertisseur de matières solides, qui contient un lit de matières solides composé de granulat contenant du carbone, en particulier un lit mobile guidé à travers la chambre de réaction, ledit lit mobile présentant au moins localement une température de l'ordre de 800 à 1700°C; fractionner le second gaz ayant la composition CnHm en carbone et en hydrogène qui constitue l'hydrogène additionnel; séparer le carbone résultant du fractionnement et l'hydrogène additionnel par dépôt du carbone sur le granulat contenant du carbone.
PCT/EP2017/058670 2016-04-28 2017-04-11 Procédé et dispositif de production de gaz de synthèse WO2017186482A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE102016005219.8 2016-04-28
DE102016005219 2016-04-28
DE102016005188.4 2016-04-29
DE102016005188.4A DE102016005188A1 (de) 2016-04-29 2016-04-29 Verfahren und Vorrichtung zur Herstellung von Synthesegas

Publications (1)

Publication Number Publication Date
WO2017186482A1 true WO2017186482A1 (fr) 2017-11-02

Family

ID=58632369

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2017/058670 WO2017186482A1 (fr) 2016-04-28 2017-04-11 Procédé et dispositif de production de gaz de synthèse

Country Status (1)

Country Link
WO (1) WO2017186482A1 (fr)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013091878A1 (fr) 2011-12-20 2013-06-27 CCP Technology GmbH Procédé et installation de conversion de dioxyde de carbone en monoxyde de carbone
WO2014097142A1 (fr) * 2012-12-21 2014-06-26 Basf Se Production en parallèle d'hydrogène, de monoxyde de carbone et d'un produit contenant du carbone
DE102013018074B3 (de) * 2013-11-28 2015-04-02 CCP Technology GmbH Hochofen und verfahren zum betrieb eines hochofens
EP2729405B1 (fr) 2011-07-05 2015-08-19 Linde Aktiengesellschaft Procédé de production de gaz de synthèse

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2729405B1 (fr) 2011-07-05 2015-08-19 Linde Aktiengesellschaft Procédé de production de gaz de synthèse
WO2013091878A1 (fr) 2011-12-20 2013-06-27 CCP Technology GmbH Procédé et installation de conversion de dioxyde de carbone en monoxyde de carbone
WO2014097142A1 (fr) * 2012-12-21 2014-06-26 Basf Se Production en parallèle d'hydrogène, de monoxyde de carbone et d'un produit contenant du carbone
DE102013018074B3 (de) * 2013-11-28 2015-04-02 CCP Technology GmbH Hochofen und verfahren zum betrieb eines hochofens

Similar Documents

Publication Publication Date Title
EP2794466B1 (fr) Procédé et installation de conversion de dioxyde de carbone en monoxyde de carbone
EP3008218B1 (fr) Haut fourneau et procédé servant à faire fonctionner un haut fourneau
DE3685559T2 (de) Zweistufiges kohlenvergasungsverfahren.
EP2729405B1 (fr) Procédé de production de gaz de synthèse
EP3194333B1 (fr) Procédé de fabrication d'un gaz de synthèse
EP2987769B1 (fr) Procédé de fabrication de gaz de synthèse et d'énergie électrique
WO2017092873A1 (fr) Procédé de production de gaz de synthèse
EP3212566B1 (fr) Procédé et installation de production de gaz de synthèse
DE69912768T2 (de) Verfahren zur herstellung von einem kohlenstoffhaltigen feststoff und wasserstoffreichen gasen
DE102014007001B4 (de) Verfahren und Anlage zur Herstellung von H2-reichem Synthesegas
EP2325288A1 (fr) Procédé et installation de traitement thermochimique et d'évaluation de substances contenant du carbone
WO2017064210A1 (fr) Dispositif et procédé de production gaz de synthèse
WO2017186482A1 (fr) Procédé et dispositif de production de gaz de synthèse
EP3143102B1 (fr) Procédé et dispositif pour la fabrication d'hydrocarbures synthétiques
DE102016005188A1 (de) Verfahren und Vorrichtung zur Herstellung von Synthesegas
DE2604140C3 (de) Verfahren zur Herstellung von Synthese- und Reduktionsgas
DE102015015968A1 (de) Verfahren zur Erzeugung von Synthesegas
DE3301962A1 (de) Verfahren zum methanisieren kohlenstoffhaltiger feststoffe
AT525654B1 (de) Verfahren zur Gewinnung von Methan aus heißem Prozessgas unter Umsetzung von kohlenstoffhaltigen Altstoffen
DE2454767C3 (de) Verfahren und Vorrichtung zur kontinuierlichen Konvertierung von Kohle in ein aus gesättigten Kohlenwasserstoffen bestehendes Gas
DE102020211407A1 (de) Verfahren und Vorrichtung zur Herstellung von Synthesegas
DE2950701C2 (fr)
WO2024023586A1 (fr) Procédé de récupération de méthane à partir de gaz de traitement chaud lors de la réaction de matériaux post-consommation contenant du carbone
DE2821413A1 (de) Teiloxydationsverfahren

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 17719201

Country of ref document: EP

Kind code of ref document: A1

122 Ep: pct application non-entry in european phase

Ref document number: 17719201

Country of ref document: EP

Kind code of ref document: A1