EP2379446A1 - Procédé de production de gaz de synthèse - Google Patents

Procédé de production de gaz de synthèse

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Publication number
EP2379446A1
EP2379446A1 EP09764738A EP09764738A EP2379446A1 EP 2379446 A1 EP2379446 A1 EP 2379446A1 EP 09764738 A EP09764738 A EP 09764738A EP 09764738 A EP09764738 A EP 09764738A EP 2379446 A1 EP2379446 A1 EP 2379446A1
Authority
EP
European Patent Office
Prior art keywords
reaction
zone
zones
reaction zone
reaction zones
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP09764738A
Other languages
German (de)
English (en)
Inventor
Ralph Schellen
Evin Hizaler Hoffmann
Leslaw Mleczko
Stephan Schubert
Rushikesh Apte
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.)
Bayer Intellectual Property GmbH
Original Assignee
Bayer Technology Services 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 Bayer Technology Services GmbH filed Critical Bayer Technology Services GmbH
Publication of EP2379446A1 publication Critical patent/EP2379446A1/fr
Withdrawn legal-status Critical Current

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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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0238—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a carbon dioxide reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1005—Arrangement or shape of catalyst
    • C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1005—Arrangement or shape of catalyst
    • C01B2203/1023—Catalysts in the form of a monolith or honeycomb
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1052—Nickel or cobalt catalysts
    • C01B2203/1058—Nickel catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1247—Higher hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • C01B2203/143—Three or more reforming, decomposition or partial oxidation steps in series
    • 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

Definitions

  • the present invention relates to a process for the endothermic, catalytic gas phase oxidation of hydrocarbons with water vapor and carbon dioxide to hydrogen and carbon monoxide (synthesis gas), wherein the reaction in 5 to 30 successive reaction zones is carried out under adiabatic conditions.
  • Synthesis gas consists essentially of carbon monoxide and hydrogen, but it can also contain carbon dioxide.
  • the essential for the production of synthesis gas from hydrocarbons partial reactions are shown in the following formulas (I to HI).
  • the formulas refer to the conversion of methane as a hydrocarbon.
  • For homologues of the hydrocarbon methane are correspondingly stoichiometrically corrected formulas, but which are also well known.
  • the reactions of formulas (I) and (HI) are highly endothermic and represent the major reactions associated with syngas production.
  • the reaction according to formula (BT) is the reaction formula known to those skilled in the art by the term "water-gas-shift reaction” and is exothermic All three reactions according to formulas (I to JH) are equilibrium-limited.
  • the synthesis gas obtained from such reactions forms an essential starting material for the further reaction, for example, to tailor-made long-chain hydrocarbons according to the Fischer-Tropsch process.
  • the controlled supply of heat in processes for the production of synthesis gas is important, since the position of the equilibria of the abovementioned reactions according to the formulas (I to JH) is strongly dependent on the temperature of the reaction zone and thus the yields and / or selectivities with respect to hydrogen and / or carbon monoxide can be controlled thereby.
  • the process variants disclosed herein relate exclusively to reactions carried out in a fired furnace, in which shell and tube reactors are located, in which the reactions are carried out. Consequently, these are not adiabatic procedures.
  • the design as a fired furnace with tube bundles is according to the method according to A.M. De Groote and G.F. Froment required.
  • A.M. De Groote and G.F. Froment discloses that this results in significant radial and axial temperature profiles in the individual reaction zones.
  • especially radial temperature profiles are disadvantageous, because in this way regions exist in regions of the reaction zones which are operated under non-optimal conditions for the reaction of the hydrocarbons to synthesis gas. A sufficient control of the temperature in the reaction zones is thus not guaranteed.
  • those of A.M. De Groote and G.F. Froment disclosed reaction devices designed extremely expensive, which is also disadvantageous, since they are at least very expensive. In case of failure but above all, a repair is possible only under Stilliegung and repair of the overall device.
  • EP 1 251 951 (B1) discloses a device and the possibility of carrying out chemical
  • Reactions in the device disclosed wherein the device is characterized by a cascade of contacting reaction zones and heat exchanger devices, which are cohesively arranged together in the composite.
  • the method to be carried out herein is thus characterized by the contact of the various
  • EP 1 251 951 (B1) is carried out in a device the same as or similar to the disclosure regarding the device.
  • the result of this is that a significant amount of heat is transferred by conduction of heat between the reaction zones and the adjacent heat exchange zones as a result of the large-area contact of the heat exchange zones with the reaction zones.
  • EP 1 251 951 (B1) discloses multi-stage processes in cascades of reaction zones from which heat in an undefined amount is removed by heat conduction.
  • the disclosed process is not adiabatic and disadvantageous in that an accurate Temperature control of the reaction is not possible. This is especially true for the undisclosed possibility of an endothermic reaction in the reaction zones.
  • Synthesis gas in the context of the present invention, denotes a process gas which essentially comprises the substances carbon monoxide and hydrogen.
  • the synthesis gas may also comprise proportions of carbon dioxide, water vapor and hydrocarbons.
  • Hydrocarbons in the context of the present invention refer to substances present as process gas consisting of carbon, hydrogen and optionally oxygen. Essentially, however, such hydrocarbons consist of carbon and hydrogen.
  • Preferred hydrocarbons which are used as feedstock in the process according to the invention are those selected from the list consisting of alkanes, alkenes and alkynes.
  • Particularly preferred hydrocarbons are alkanes.
  • Preferred alkanes are those comprising at most six carbon atoms, more preferably methane, ethane, propane and butane, most preferably methane.
  • steam refers to a process gas which essentially comprises water in the gaseous state.
  • the term essentially refers in the context of the present invention, a mass fraction and / or a molar fraction of at least 80%.
  • hydrocarbons used in the process according to the invention, the steam, the constituents of the synthesis gas and the synthesis gas as such, will also be referred to collectively below as process gases.
  • adiabatic conditions means that the reaction zone from the outside is essentially neither actively supplied with heat nor heat withdrawn. It is well known that complete isolation against heat input or removal is possible only by complete evacuation to the exclusion of the possibility of heat transfer by radiation. Therefore, in the context of the present invention, adiabat means that no heat supply or removal measures are taken.
  • An advantage of the adiabatic driving method according to the invention of the 5 to 30 reaction zones connected in series with respect to a non-adiabatic driving mode is that no means for supplying heat must be provided in the reaction zones, which entails a considerable simplification of the construction. This results in particular simplifications in the manufacture of the reactor and in the scalability of the process and an increase in reaction conversions.
  • Another advantage of the method according to the invention is the possibility of very accurate temperature control by the close staggering of adiabatic reaction zones. It can thus be set and controlled in each reaction zone advantageous in the reaction progress temperature.
  • Yet another advantage of the process of the invention is that, unlike the prior art processes discussed above, the addition of carbon dioxide produces the desired synthesis gas, i. an increased proportion of carbon monoxide is generated. In the prior art processes, predominantly hydrogen is produced which is also a component of the synthesis gas. However, by the supply of carbon dioxide, the ratio of hydrogen to carbon monoxide can be controlled as desired.
  • the catalysts used in the process according to the invention are usually catalysts which consist of a material which, in addition to its catalytic activity for the reaction according to the formers (I to JE), is characterized by sufficient chemical resistance under the conditions of the process and by a high specific surface area .
  • Catalyst materials characterized by such chemical resistance under the conditions of the process are, for example, catalysts comprising nickel or nickel compounds.
  • Such catalysts can be applied to support materials.
  • Such support materials usually include alumina, calcia, magnesia, silica and / or titania.
  • Carrier materials of magnesium spinels are preferred.
  • Specific surface area in the context of the present invention refers to the area of the catalyst material that can be reached by the process gases, based on the mass of catalyst material used.
  • a high specific surface area is a specific surface area of at least 1 m 2 / g, preferably of at least 10 m 2 / g.
  • the catalysts of the invention are each in the reaction zones and can be used in all known forms, e.g. Fixed bed, moving bed, present.
  • the appearance is fixed bed.
  • the fixed bed arrangement comprises a catalyst bed in the true sense, d. H. loose, supported or unsupported catalyst in any form and in the form of suitable packings.
  • catalyst bed as used herein also encompasses contiguous areas of suitable packages on a support material or structured catalyst supports. These would be e.g. to be coated ceramic honeycomb carrier with comparatively high geometric surfaces or corrugated layers of metal wire mesh on which, for example, catalyst granules is immobilized.
  • a special form of packing in the context of the present invention, the presence of the catalyst in monolithic form is considered. Such monolithic forms may also be foams of a carrier material on which the aforementioned catalyst materials have been applied.
  • the catalyst is preferably present in beds of particles having mean particle sizes of 1 to 10 mm, preferably 2 to 8 mm, particularly preferably 3 to 7 mm.
  • the catalyst is in a fixed bed arrangement in monolithic form.
  • a monolithic catalyst comprising nickel compounds supported on magnesium spinels.
  • the monolithic catalyst is provided with channels through which the process gases flow.
  • the channels have a diameter of 0.1 to 3 mm, preferably a diameter of 0.2 to 2 mm, more preferably from 0.5 to 1.5 mm.
  • the catalyst is preferably present in loose beds of particles, as have already been described in connection with the fixed bed arrangement.
  • the conversion takes place in 7 to 20, more preferably 10 to 15 reaction zones connected in series.
  • a preferred further embodiment of the method is characterized in that the process gas emerging from at least one reaction zone is subsequently passed through at least one heat exchange zone downstream of said reaction zone.
  • each reaction zone is at least one, preferably exactly one heat exchange zone, through which the process gas leaving the reaction zone is passed.
  • the reaction zones can either be arranged in a reactor or arranged divided into several reactors.
  • the arrangement of the reaction zones in a reactor leads to a reduction in the number of apparatuses used.
  • the individual reaction zones and heat exchange zones can also be arranged together in a reactor or in any combination of reaction zones with heat exchange zones in several reactors.
  • reaction zones and heat exchange zones are present in a reactor, then in an alternative embodiment of the invention there is a heat insulation zone between them, in order to be able to obtain the adiabatic operation of the reaction zone.
  • each of the series-connected reaction zones can be replaced or supplemented independently of one another by one or more reaction zones connected in parallel.
  • the use of reaction zones connected in parallel allows in particular their replacement or supplementation during ongoing continuous operation of the process.
  • Parallel and successive reaction zones may in particular also be combined with one another.
  • the process according to the invention particularly preferably has exclusively reaction zones connected in series.
  • the reactors preferably used in the process according to the invention can consist of simple containers with one or more reaction zones, as e.g. in Ullmann's Encyclopedia of Industrial Chemistry (Fifth, Completely Revised Edition, VoI B4, page 95-104, page 210-216), wherein in each case between the individual reaction zones and / or heat exchange zones heat insulation zones can be additionally provided.
  • the catalysts or the fixed beds thereof are mounted in a manner known per se on or between gas-permeable walls comprising the reaction zone of the reactor. Particularly in the case of thin fixed beds, technical devices for uniform gas distribution can be provided in the flow direction in front of the catalyst beds. These can be perforated plates or other internals that cause a uniform entry of the process gas into the fixed bed by generating a small but uniform pressure loss.
  • the inlet temperature of the process gas entering the first reaction zone is from 700 to 1000 ° C., preferably from 800 to 950 ° C., particularly preferably from 850 to 900 ° C.
  • the absolute pressure at the inlet of the first reaction zone is between 10 and 40 bar, preferably between 20 and 35 bar, particularly preferably between 25 and 30 bar.
  • the residence time of the process gas in all reaction zones together is between 0.05 and 20 s, preferably between 0.1 and 5 s, particularly preferably between 0.5 and 3 s.
  • the hydrocarbon, the carbon dioxide and the water vapor are preferably fed only before the first reaction zone.
  • This has the advantage that the entire process gas is available for absorbing heat of reaction in all reaction zones.
  • the space-time yield can be increased, or the necessary catalyst mass can be reduced.
  • the temperature and the conversion can be controlled via the supply of these process gases between the reaction zones.
  • the process gases may also be preheated.
  • the process gas is heated after at least one of the reaction zones used, more preferably after each reaction zone.
  • the process gas is passed after exiting a reaction zone through one or more of the above-mentioned heat exchange zones, which are located behind the respective reaction zones.
  • These may be used as heat exchange zones in the form of heat exchangers known to those skilled in the art, e.g. Tube bundle, plate, Ringnut-, spiral, finned tube, micro-heat exchanger be executed.
  • the heat exchangers are preferably microstructured heat exchangers.
  • microstructured means that the heat exchanger for the purpose of heat transfer comprises fluid-carrying channels, which are characterized in that they have a hydraulic diameter between 50 ⁇ m and 5 mm.
  • the hydraulic diameter is calculated as four times the flow cross-sectional area of the fluid-conducting channel divided by the circumference of the channel.
  • the heating of the process gas takes place in the heat exchange zones by a condensation of a heat transfer medium.
  • condensation preferably partial condensation, in the heat exchangers containing the heat exchange zones on the side of the heating medium.
  • Partial condensation referred to in the context of the present invention, a condensation in which a gas / liquid mixture of a substance is used as a heating medium and in which there is still a GasTFlüsstechniksgemisch this substance after heat transfer in the heat exchanger.
  • the execution of a condensation is particularly advantageous because in this way the achievable heat transfer coefficient to the process gases from the heating medium is particularly high and thus efficient heating can be achieved.
  • Performing a partial condensation is particularly advantageous because the release of heat by the heating medium thereby no longer results in a change in temperature of the heating medium, but only the gas-liquid equilibrium is shifted. This has the consequence that over the entire heat exchange zone, the process gas is heated to a constant temperature. This in turn safely prevents the occurrence of radial temperature profiles in the flow of process gases, thereby improving control over the reaction temperatures in the reaction zones and, in particular, preventing the formation of local overheating by radial temperature profiles.
  • a condensation / partial condensation instead of a condensation / partial condensation, it is also possible to provide a mixing zone upstream of the inlet of a reaction zone in order to standardize the radial temperature profiles, if appropriate during the heating, in the flow of the process gases by mixing transversely to the main flow direction.
  • the reaction zones connected in series are operated at an average temperature increasing or decreasing from reaction zone to reaction zone. This means that within a sequence of reaction zones, the temperature can be both increased and decreased from reaction zone to reaction zone. This can be adjusted, for example, via the control of the heat exchange zones connected between the reaction zone. Further options for setting the average temperature are described below.
  • the thickness of the flow-through reaction zones can be chosen to be the same or different and results according to laws generally known in the art from the residence time described above and the process gas quantities enforced in the process.
  • the inventively enforceable with the method mass flows of product gas (Carbon monoxide), which also results in the process gas quantities to be used, are usually between 5 and 10 t / h, preferably between 7 and 8 t / h, more preferably between 7.3 and 7.4 t / h.
  • the maximum outlet temperature of the process gas from the first reaction zone is usually in a range from 500 ° C. to 850 ° C., preferably from 650 ° C. to 800 ° C., more preferably from 700 ° C. to 750 ° C. subsequent measures with regard to their inlet temperature by the skilled person, are determined freely according to the inventive method.
  • the control of the temperature in the reaction zones preferably takes place by at least one of the following measures: dimensioning of the adiabatic reaction zone, control of the heat supply between the reaction zones, addition of further process gas between the reaction zones, molar ratio of the educts / excess of water vapor used and / or carbon dioxide, Addition of secondary constituents, in particular nitrogen, before and / or between the reaction zones.
  • composition of the catalysts in the reaction zones according to the invention may be identical or different. In a preferred embodiment, the same catalysts are used in each reaction zone. However, it is also advantageous to use different catalysts in the individual reaction zones.
  • a less active catalyst can be used and in the further reaction zones the activity of the catalyst can be increased from reaction zone to reaction zone.
  • the control of the catalyst activity can also be carried out by dilution with inert materials or carrier material.
  • the erf ⁇ ndungshiele method is thus characterized by high space-time yields, combined with a reduction in the size of the apparatus and a simplification of the apparatus or reactors.
  • This surprisingly high space-time yield is made possible by the interaction of the erf ⁇ ndungswashen and preferred embodiments of the new method.
  • the interaction of staggered adiabatic reaction zones with interposed heat exchange zones and the defined residence times allows accurate Control of the process and the resulting high space-time yields, as well as a reduction of the by-products formed.
  • Fig. 1 shows reactor temperature (T) and methane conversion (U) over a number of 12 reaction zones (S) with downstream heat exchange zones (according to Example 1).
  • a process gas consisting of water vapor, methane and carbon dioxide is fed to the process.
  • the molar ratio of methane to carbon dioxide is 1: 1 and the molar ratio of methane to water vapor is 1: 2.
  • the process is in a total of 12 fixed catalyst beds of magnesium spinel coated with nickel, wherein a proportion of 15.2 wt .-% of nickel is present on the catalyst, ie in 12 reaction zones operated.
  • composition of the process gas used at the beginning of the first reaction zone causes the reactions according to the formulas (II and III) to be strongly forced to the left equilibrium side. This is especially true for the reaction according to formula (H).
  • Each after a reaction zone is a heat exchange zone in which the exiting process gas is reheated before it enters the next reaction zone.
  • the absolute inlet pressure of the process gas directly in front of the first reaction zone is 29 bar.
  • the length of the fixed catalyst beds, ie the reaction zones, is always 0.1 m.
  • the activity of the catalyst used is not variable across the reaction zones.
  • the proportion catalyst volume per total volume of each reaction zone is always 25 vol .-%.
  • the total residence time in the plant is 0.6 seconds.
  • the results are shown in FIG.
  • the individual reaction zones are listed on the x-axis, so that a spatial course of developments in the process is visible.
  • the temperature of the process gas is indicated on the left y-axis.
  • the temperature profile across the individual reaction zones is shown as a thick, solid line.
  • On the right y-axis the total conversion of methane is indicated.
  • the course of the conversion over the individual reaction zones is shown as a thick dashed line.
  • the inlet temperature of the process gas before the first reaction zone is about 900 ° C. Due to the substantially endothermic reaction to synthesis gas under adiabatic conditions, the temperature in the first reaction zone drops to about 735 ° C before the process gas is reheated in the downstream heat exchange zone. The inlet temperature before the next reaction zone is again about 900 0 C. By endothermic adiabatic reaction, it decreases again to about 780 0 C. The sequence of cooling by endothermic, adiabatic reaction and heating continues with successively increasing inlet temperatures before the respective reaction zones. The inlet temperature of the process gas before the last reaction zone thus changes in the course of the process to a value of about 850 ° C. It is obtained a conversion of methane of 74.8%.
  • the space-time yield achieved, based on the mass of catalyst used, is 3.99 kg K ⁇ h enemone ⁇ id / kg ⁇ ath.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Industrial Gases (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne un procédé de production d'hydrogène et de monoxyde de carbone (le gaz de synthèse) par oxydation d'hydrocarbures en phase gazeuse par voie endothermique et catalytique, au moyen de vapeur d'eau et de dioxyde de carbone, la transformation s'effectuant dans des conditions adiabatiques dans 5 à 30 zones de réaction successives.
EP09764738A 2008-12-20 2009-12-04 Procédé de production de gaz de synthèse Withdrawn EP2379446A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008064277A DE102008064277A1 (de) 2008-12-20 2008-12-20 Verfahren zur Herstellung von Synthesegas
PCT/EP2009/008670 WO2010069485A1 (fr) 2008-12-20 2009-12-04 Procédé de production de gaz de synthèse

Publications (1)

Publication Number Publication Date
EP2379446A1 true EP2379446A1 (fr) 2011-10-26

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP09764738A Withdrawn EP2379446A1 (fr) 2008-12-20 2009-12-04 Procédé de production de gaz de synthèse

Country Status (4)

Country Link
US (1) US8758647B2 (fr)
EP (1) EP2379446A1 (fr)
DE (1) DE102008064277A1 (fr)
WO (1) WO2010069485A1 (fr)

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Publication number Priority date Publication date Assignee Title
RU2478078C1 (ru) * 2011-09-14 2013-03-27 Открытое акционерное общество "Газпром" Способ получения метановодородной смеси

Family Cites Families (6)

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Publication number Priority date Publication date Assignee Title
US3278452A (en) * 1959-12-24 1966-10-11 Pullman Inc Production of hydrogen-containing gases
FR2560866B1 (fr) 1984-03-09 1988-05-20 Inst Francais Du Petrole Nouveau procede de fabrication de gaz de synthese par oxydation indirecte d'hydrocarbures
EP1251951B2 (fr) 2000-01-25 2014-10-29 Meggitt (U.K.) Limited Reacteur chimique comportant un echangeur de chaleur
US6773580B2 (en) * 2001-12-11 2004-08-10 Corning Incorporated Catalytic reforming system and process
AUPR981702A0 (en) * 2002-01-04 2002-01-31 Meggitt (Uk) Limited Steam reformer
US7686856B2 (en) * 2006-06-19 2010-03-30 Praxair Technology, Inc. Method and apparatus for producing synthesis gas

Non-Patent Citations (1)

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Title
See references of WO2010069485A1 *

Also Published As

Publication number Publication date
US20110240925A1 (en) 2011-10-06
DE102008064277A1 (de) 2010-07-01
US8758647B2 (en) 2014-06-24
WO2010069485A8 (fr) 2011-05-05
WO2010069485A1 (fr) 2010-06-24

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