EP4204386A1 - Procédé et installation pour produire un ou plusieurs hydrocarbures - Google Patents

Procédé et installation pour produire un ou plusieurs hydrocarbures

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Publication number
EP4204386A1
EP4204386A1 EP21806224.8A EP21806224A EP4204386A1 EP 4204386 A1 EP4204386 A1 EP 4204386A1 EP 21806224 A EP21806224 A EP 21806224A EP 4204386 A1 EP4204386 A1 EP 4204386A1
Authority
EP
European Patent Office
Prior art keywords
reaction zone
reaction
process gas
gas stream
catalysts
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.)
Pending
Application number
EP21806224.8A
Other languages
German (de)
English (en)
Inventor
Andreas Meiswinkel
Hans-Jörg ZANDER
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.)
Linde GmbH
Original Assignee
Linde 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 Linde GmbH filed Critical Linde GmbH
Publication of EP4204386A1 publication Critical patent/EP4204386A1/fr
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0455—Reaction conditions
    • C07C1/0475—Regulating
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/12—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon dioxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/1516—Multisteps
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
    • 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
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the present invention relates to a method for producing one or more hydrocarbons, in particular ethylene and/or propylene, and a corresponding plant according to the preambles of the independent patent claims.
  • Ethylene and propylene are essential building blocks in petrochemistry. Further continuous growth is expected for both products. Annual demand in 2016 was 150 million t/a for ethylene (capacity 170 million t/a) and 100 million t/a for propylene (capacity 120 million t/a). In particular, an increasing demand for propylene (“propylene gap”) is forecast, which requires the provision of corresponding selective processes.
  • the invention therefore aims at an improved process for the production of hydrocarbons from carbon dioxide.
  • the aim of the invention is in particular the production of paraffins and particularly preferably of olefins.
  • the invention is particularly on the production of Paraffins and olefins having two to eight carbon atoms, but especially two and three carbon atoms, directed. Accordingly, the following explanations are in part strongly geared towards the production of ethylene and propylene. Aromatics can also be formed as by-products.
  • the present invention is not limited to these hydrocarbons.
  • the present invention applies in particular to processes which currently lead to hydrocarbons via methanol and/or dimethyl ether as an (isolated) intermediate stage.
  • This relates to the synthesis of methanol and/or dimethyl ether from synthesis gas, which is explained in more detail below, followed by the methanol-to-olefins or methanol-to-propylene processes, which are also explained in more detail below.
  • these processes are carried out in two stages, i.e. sequentially in separate reaction steps and over different catalysts.
  • the object of the present invention is to improve corresponding methods and in particular to design them more advantageously with regard to their energy consumption and/or carbon dioxide footprint. Disclosure of Invention
  • the present invention proposes a method for producing one or more hydrocarbons, in particular ethylene and/or propylene, and a corresponding plant with the respective features of the independent patent claims.
  • Preferred embodiments of the present invention are the subject matter of the dependent patent claims and the following description.
  • the invention begins with processes which currently lead to hydrocarbons via methanol and/or dimethyl ether as an (isolated) intermediate stage and which are explained in detail further below.
  • olefins such as ethylene and propylene
  • olefins such as ethylene and propylene
  • steam cracking in which case inputs such as ethane, propane, so-called liquefied petroleum gas (LPG) or naphtha can be used, and, in particular for the production of propylene, fluid catalytic cracking using an appropriate catalyst.
  • LPG liquefied petroleum gas
  • propylene fluid catalytic cracking using an appropriate catalyst.
  • ethylene alternatives technologies for the production of ethylene include the fundamentally known oxidative dehydrogenation of ethane (ODH-E), in which acetic acid is formed as a by-product, and the also known oxidative coupling of methane.
  • Processes for the production of propylene include, for example, the established propane dehydrogenation and olefin metathesis, which requires 2-butene as an input.
  • modified Fischer-Tropsch processes optimized to produce a maximum yield of light olefins (“Fischer-Tropsch-To-Olefins", FTTO) and Fischer-Tropsch processes combined with a reverse water gas shift (RWGS). are, so that carbon dioxide can also be incorporated, can be mentioned here.
  • specialist literature such as [8] and [9] on FTTO and [10] to [12] on the combination of Fischer-Tropsch methods with RWGS.
  • methanol-to-olefins or methanol-to-propylene processes mentioned usually start from methanol and/or dimethyl ether as an isolated intermediate stage, which is produced by converting synthesis gas (e.g. generated from methane, but also from coal, naphtha, etc.) can be made.
  • olefins such as ethylene and propylene are sought as the preferred target product.
  • Lewis acidic materials, in particular zeolites or are used as catalysts zeolite-like materials used. By choosing the catalyst material and the exact reaction conditions, the product spectrum can be adjusted, especially with regard to the type of products and their relative distribution.
  • zeolites basic type ZSM-5, medium porosity
  • SAPO silicoaluminophosphates
  • SAPO-34 low porosity
  • Methanol-to-olefins or methanol-to-propylene processes are commercially established and are used, for example, in the form of a methanol-to-propylene process based on a zeolite catalyst and a fixed-bed reactor (one or two reactor systems with an additional reserve reactor are common) and in the form of a methanol-to-olefins process with a catalyst based on SAPO-34.
  • a main advantage is said to be the simple possibility of expanding the fixed-bed reactor (parallelization) and the significantly lower investment costs, the main aim being propylene as the target product, but significant amounts of heavier fractions are also formed.
  • the advantage of the latter is said to be that in SAPO-34 compared to ZSM-5 there are narrower microcrystalline pores and better control of the acidity can be achieved.
  • Crude methanol is typically used in the latter process and the reactor system used comprises two fluidized bed reactors (one for the actual reaction and one for continuous catalyst regeneration), the process being characterized by temperature, at 350 to 525 O (preferably 350 O), pressure at 1 to 3 barg, the residence time and the regeneration cycle is controlled.
  • OCP Olefins Cracking Process
  • the bifunctional catalysts catalyze two reaction steps, namely conversion of the components of synthesis gas to one or more oxygenates such as methanol and/or dimethyl ether as intermediate(s) and further conversion of the intermediate(s) to the desired target compound in the form of one or more hydrocarbons .
  • a bifunctional catalyst used here combines typically used methanol catalysts with acidic zeolite structures which catalyze the subsequent reaction.
  • the two reaction steps can also take place in parallel using a combination of two or more suitable catalysts, each of which preferably catalyzes the corresponding reaction steps, as a physical mixture in a catalyst bed.
  • suitable catalysts can be the above-mentioned catalysts for methanol or dimethyl ether synthesis or for further conversion, which are known in principle.
  • the overall reaction takes place in both variants when viewed externally as a one-stage reaction, which, however, comprises two individual reactions or reaction steps.
  • bifunctional catalysts used for converting carbon dioxide are given in Table 1 below.
  • the invention proposes a combination of the two reaction steps mentioned in one reactor or in several reactors with a suitable catalyst (where one or both of the reaction steps according to the above equations (1) and (2) as a first reaction step and the reaction step 3 according to the above Equation (3) is interpreted as the second reaction step.
  • the reactions involved are basically thermodynamically limited equilibrium reactions. From this it follows that in principle all species involved (educts such as carbon monoxide, carbon dioxide and hydrogen, intermediates such as methanol and/or dimethyl ether and hydrocarbons as products such as in particular ethylene and propylene) are present in the reaction matrix at all times. In addition to the reaction kinetics, the corresponding proportion is determined in particular by the thermodynamic equilibrium position. In particular at the reactor outlet, the composition should increasingly approach this thermodynamic equilibrium.
  • FIG. 2A illustrates the conversion X eq in percent for the case that the reactions are successively brought to equilibrium, on the vertical axis compared to a pressure p in bar on the horizontal axis shown on the left and a temperature in G on the horizontal axis shown on the right .
  • FIG. 2B illustrates the conversion X eq for the case in which both reactions are brought into equilibrium simultaneously.
  • the present invention proposes a method in which carbon dioxide and / or carbon monoxide are reacted with hydrogen in a process gas stream that is fed to a reactor, at least in part in a first reaction step to form one or more oxygenates, the or in the Process gas stream pass over, and in which the one or more oxygenates in the process gas stream is or are converted at least in part in a second reaction step to form the one or more hydrocarbons, which pass into the process gas stream, the process gas stream flowing through in one flow direction a reactor assembly is performed.
  • a “reactor arrangement” is to be understood as an arrangement that has one or more reactors and the components required for their operation as minimum equipment.
  • the reactor arrangement comprises one or more reactors which has or have a first and a second reaction zone, the second reaction zone being arranged downstream of the first reaction zone in the direction of flow, and the first reaction zone and the second reaction zone being arranged in such a way are equipped with catalysts, that in the first reaction zone the first and the second reaction step are catalyzed, that in the second reaction zone the second reaction step is catalysed, and that in the second reaction zone the first reaction step does not occur or to a lesser extent than in the first reaction zone is catalyzed.
  • a “lesser extent” is understood to mean, for example, a relative conversion of an amount of substance of less than 10%, in particular 5% and in particular 2%, of the amount of substance converted in the first reaction zone in the first reaction step.
  • the first and second reaction zones can be located in one reactor of the reactor arrangement, or two reactors can be provided which have the two reaction zones in the arrangement mentioned one behind the other.
  • “one” reactor is mentioned below.
  • a second reaction zone in which predominantly or exclusively one or more oxygenates such as methanol and/or dimethyl ether is or are being reacted, but not carbon dioxide, carbon monoxide and hydrogen, but which are further in the Process gas stream are included in a first reaction zone in which, in addition to the implementation of one or more oxygenates, the conversion of carbon dioxide, carbon monoxide and hydrogen to the oxygenates also takes place.
  • the process gas in the second reaction zone is depleted of the one or more oxygenates, which also facilitates the subsequent processing, as explained in more detail below.
  • the first reaction zone can, in the present context, be equipped with one or more first catalysts, which catalyzes or catalyze the first reaction step, and with one or more second catalysts, which catalyzes or catalyzes the second reaction step, for example in the form of a physical mixture.
  • first catalysts which catalyzes or catalyze the first reaction step
  • second catalysts which catalyzes or catalyzes the second reaction step
  • a bifunctional catalyst without the use of the measures proposed according to the invention, or even the pure use of two catalysts simultaneously, ie in one catalyst bed, also has a disadvantage for the technical Use on. Since, as mentioned, complete conversion of carbon monoxide and carbon dioxide cannot be achieved in technically relevant systems, one or more oxygenates are continuously formed in accordance with the thermodynamic equilibrium by such a bifunctional catalyst or a corresponding mixture, which or the thus is or are present in significant amounts (at least in the percentage range) in the effluent of a respective reactor.
  • the one or more oxygenates are converted together with the water of reaction into a condensate from which the condensate or condensates, in particular methanol, can only be separated off and put to use with comparatively great effort. So there is inevitably a undesired by-product that is hardly economically separable or usable. As a result, this by-product is usually fed into a wastewater treatment system with the condensate and is thus lost from the value chain.
  • methanol can be broken down by suitable bacteria in biological wastewater treatment, which in turn results in the emission of carbon dioxide.
  • this degradation of methanol in biological sewage treatment plants is in principle technically possible without further ado, it means additional effort here (because of the capacity to be provided for the biological treatment).
  • a separation or subsequent waste water treatment is no longer necessary or a lower capacity is sufficient here, since the one or more oxygenates are reacted in the second reaction zone.
  • the content of oxygenate(s) at the reactor outlet can be effectively minimized and thus the process efficiency in the direction of the target products can be significantly increased.
  • Other components such as carbon monoxide, carbon dioxide and hydrogen can then be separated from the target products and recycled relatively easily.
  • one or more further reaction zones containing suitable catalysts which in particular catalyze a water gas shift reaction and/or the formation of methanol and/or dimethyl ether as an intermediate can also be arranged upstream of the first reaction zone according to the invention.
  • suitable catalysts which in particular catalyze a water gas shift reaction and/or the formation of methanol and/or dimethyl ether as an intermediate.
  • the further conversion to hydrocarbons according to the above definition is not catalyzed or only to a “lesser extent” than in the first reaction zone.
  • reactors are suitable for carrying out the reaction with heterogeneous catalysts.
  • Fixed-bed reactors as described for example in [40] and [41], are particularly advantageous since they are structurally comparatively easy to implement.
  • the reactor used in the context of the present invention is therefore designed as a fixed-bed reactor which has fixed catalyst beds in the first reaction zone and in the second reaction zone, which contain the respective catalysts as fixed-bed catalysts. The same applies if several reactors are used or in one corresponding reactor arrangement are included.
  • a "catalyst bed” typically has a supported catalyst in a suitable support structure.
  • tube bundle reactors with a suitable cooling medium in particular a molten salt
  • a suitable cooling medium in particular a molten salt
  • the cooling can take place in co-current or counter-current with the process gas flow, and different cooling/heating zones can also be provided within the scope of the invention, if required.
  • the reaction zones provided according to the invention are formed by separate catalyst beds arranged in parallel in the reaction tubes, or such catalyst beds together form the reaction zones in each case. It goes without saying that when, in simplified terms, "a process gas stream" is passed through the reactor or a corresponding reactor arrangement, in the case of a tube bundle reactor this refers to a number of partial streams corresponding to the number of reaction tubes.
  • Adiabatic fixed-bed reactors are known, which can optionally also be designed in a multi-stage design with intermediate coolers.
  • heated or cooled reactors which are typically designed as tube bundle reactors, are known, in particular for strongly endothermic or exothermic reactions.
  • systems with a phase change e.g. water/steam or other evaporating liquids
  • thermal oils or, especially at higher temperatures, molten salts are used as the cooling/heating medium.
  • the temperature control can take place in co-current or counter-current, and in more recent designs different cooling/heating zones are also provided in the design.
  • multilayer catalyst beds or beds in a fixed bed reactor is also known.
  • multilayer catalyst beds can be used in conventional processes, optionally with increasing activity along the direction of flow in the reactor.
  • DE10 2005 004 926 A1 describes a catalyst system for catalytic gas-phase reactions which is characterized by increasing catalyst activity in the direction of flow.
  • Activity increase achieved exclusively by mixtures of different active catalysts, but which basically catalyze the same reaction.
  • the production of phthalic anhydride, ethylene dichloride, cyclohexanone, maleic anhydride and acrylic acid is mentioned in particular as a method.
  • a continuous gradient is expressly suggested and not the use of different defined zones.
  • EP 3 587383 A1 relating to oxidative dehydrogenation, also uses a reactor which has a plurality of reaction zones, each with a catalyst bed.
  • the several reaction zones can be designed in particular as a layered structure made up of several catalyst beds or as reaction zones which are separate from one another and each have one catalyst bed.
  • the catalyst loading and/or catalyst activity is adjusted in particular by different degrees of dilution using inert material, but the active catalyst material in the different reaction zones is identical and therefore basically catalyzes the same reactions.
  • the first reaction zone advantageously has a plurality of catalyst beds which are arranged one behind the other in the direction of flow and have a plurality of different catalysts or one catalyst with different activity.
  • This can also relate to a bifunctional catalyst, as can be provided in the first reaction zone. Mixtures of catalysts in different mixing proportions can also be provided.
  • a plurality of catalyst-free inert zones are advantageously also formed in the direction of flow. These can be, for example, before the first and after the second reaction zone. Further inert beds can also be arranged between the reaction beds and/or individual catalyst beds in order, for example, to achieve better heat dissipation or temperature control.
  • catalysts which are generally known for the respective reaction system can be considered without restriction. Reference is made to the above explanations, in particular in connection with Table 1. the The invention is characterized less by the types of catalysts used than by the reactions catalyzed by them and the order and specific type of arrangement of the catalysts used.
  • the process according to the invention can be carried out at a pressure level of 10 to 100 bar, in particular 12 to 50 bar, more particularly 15 to 35 bar, and a temperature level of 150 to 580°, in particular 200 to 450°, more particularly 250 to 400° will.
  • the process according to the invention is suitable for the reaction of carbon dioxide and carbon monoxide and gas streams with any mixtures of these two components.
  • hydrogen is to be provided in a suitable stoichiometric amount in the reaction feed.
  • the index S N the so-called stoichiometric modulus, is helpful and common for determining the required proportion of hydrogen in corresponding reactions. It is determined from the mole fractions x of carbon monoxide, carbon dioxide and hydrogen as follows:
  • Equations 6 and 7 below describe the idealized synthesis of ethylene.
  • S N 2 always applies.
  • An upper limit for S N is also advantageous in order to limit the effort required to separate and recycle hydrogen and, on the other hand, to avoid an overreaction of olefins to form the corresponding paraffins ("hydrogenation").
  • the process gas stream of the reactor arrangement used in the invention is therefore advantageously fed with a stoichiometric modulus of 1.5 to 10, in particular 2 to 4.
  • the one or more oxygenates are in particular methanol and/or dimethyl ether and the one or more hydrocarbons are in particular ethylene and propylene.
  • the present invention is also suitable for other methods of carbon monoxide and/or carbon dioxide hydrogenation, i.e. in particular also the production of higher hydrocarbons having four or more carbon atoms.
  • the process gas stream can also have other components, in particular methane and/or higher hydrocarbons, in addition to the components mentioned, hydrogen, carbon dioxide and/or carbon monoxide, when it enters the reactor arrangement.
  • the plant according to the invention for the production of one or more hydrocarbons, in particular ethylene and/or propylene, is set up to combine carbon dioxide and/or carbon monoxide with hydrogen in a process gas stream which is fed to a reactor arrangement, at least in part in a first reaction step to form one or converting a plurality of oxygenates which pass into the process gas stream, and converting the one or more oxygenates in the process gas stream at least in part in a second reaction step into the one or more hydrocarbons which pass into the process gas stream.
  • the plant is set up to guide the process gas stream through the reactor arrangement in a direction of flow, the reactor arrangement having one or more reactors which comprise or comprise a first reaction zone and a second reaction zone, the second reaction zone being downstream in the direction of flow first reaction zone is arranged, and wherein the first reaction zone and the second reaction zone are equipped with catalysts in such a way that the first and the second reaction step are catalyzed in the first reaction zone, that the second reaction step is catalyzed in the second reaction zone, and that in the second Reaction zone, the first reaction step is not catalyzed or to a lesser extent than in the first reaction zone.
  • the present invention achieves a particularly efficient conversion of carbon monoxide and/or carbon dioxide with hydrogen to products of value.
  • the conversion or the yield is maximized compared to conventional processes.
  • An integrated procedure is achieved without isolating the intermediate or the intermediates.
  • intermediates such as methanol and/or dimethyl ether as (unused) by-products in the effluent.
  • the process efficiency towards the desired target products increases. No complex methanol recovery is required and the requirements for wastewater treatment (biology) are minimized. Overall, there is a reduction in construction and operating costs.
  • FIG. 1 shows a method according to an embodiment of the invention.
  • FIGS. 2A and 2B illustrate advantages of an embodiment of the invention over the prior art using conversion diagrams.
  • FIG. 1 a method according to a particularly preferred embodiment of the present invention is illustrated in the form of a schematic flowchart and denoted overall by 100.
  • the following explanations relate to a system according to an embodiment of the invention in the same way.
  • carbon dioxide and/or carbon monoxide is reacted with hydrogen in a process gas stream 1, which is fed to a reactor 10, at least in part in a first reaction step to form one or more oxygenates, which pass into the process gas stream 1, and the one or more oxygenates in the process gas stream 1 is or are at least partly converted into one or more hydrocarbons in a second reaction step, which or which pass into the process gas stream 1 .
  • a reactor 10 instead of one reactor 10, an arrangement with several reactors can also be used within the scope of the invention.
  • the process gas stream 1 is guided in a flow direction through the reactor 10, the reactor 10 having a first reaction zone 11 and a second reaction zone 12, the second Reaction zone 12 is arranged downstream of the first reaction zone 11 in the direction of flow, with the first reaction zone 11 in the example shown having one or more bifunctional catalysts that catalyze the first and second reaction step, and the second reaction zone 12 having one or more predominantly or exclusively the second reaction step having catalyzing catalysts.
  • the one or more bifunctional catalysts it is also possible, for example, to use a mixture of a plurality of catalysts, as mentioned.
  • a “bifunctional” catalyst is described in the first reaction zone and a “monofunctional” catalyst in the second reaction zone in the description of the figures.
  • a fixed-bed reactor is used as reactor 10, which has a plurality of catalyst beds 11a, 11b, 11c in the first reaction zone 11, which contain the one or more bifunctional catalysts as fixed-bed catalyst or fixed-bed catalysts, and which has a catalyst bed in the second reaction zone 12 12a, which contains the one or more monofunctional catalysts as a fixed bed catalyst or fixed bed catalysts.
  • Further zones 14 can be provided and equipped accordingly with a catalyst.
  • Catalyst-free inert zones 13 are formed upstream of the first and downstream of the second reaction zone.

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

Abstract

L'invention concerne un procédé (100) pour produire un ou plusieurs hydrocarbures, selon lequel on fait réagir au moins partiellement du dioxyde de carbone et/ou du monoxyde de carbone dans une première étape de réaction avec de l'hydrogène dans un flux de gaz de traitement (1), qui est introduit dans un ensemble réacteur, pour donner un ou plusieurs composés oxygénés qui passent dans le flux de gaz de traitement (1), et le ou les composés oxygénés dans le flux de gaz de traitement (1) est ou sont au moins partiellement mis à réagir dans une seconde étape de réaction pour donner un ou plusieurs hydrocarbures qui passent dans le flux de gaz de traitement (1). Le flux de gaz de traitement (1) est guidé dans une direction d'écoulement à travers l'ensemble réacteur et l'ensemble réacteur comprend un ou plusieurs réacteurs (10) qui a ou qui ont une première zone de réaction (11) et une seconde zone de réaction (12). La seconde zone de réaction (12) est située en aval de la première zone de réaction (11) dans la direction d'écoulement, et la première zone de réaction (11) et la seconde zone de réaction (12) sont équipées de catalyseurs de sorte que : les première et seconde étapes de réaction sont catalysées dans la première zone de réaction (11) ; la seconde étape de réaction est catalysée dans la seconde zone de réaction ; et la première étape de réaction n'est pas catalysée dans la seconde zone de réaction (12), ou est catalysée dans une moindre mesure que dans la première zone de réaction (11). La présente invention concerne également une installation correspondante.
EP21806224.8A 2020-11-06 2021-11-04 Procédé et installation pour produire un ou plusieurs hydrocarbures Pending EP4204386A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102020129303.8A DE102020129303A1 (de) 2020-11-06 2020-11-06 Verfahren und Anlage zur Herstellung eines oder mehrerer Kohlenwasserstoffe
PCT/EP2021/080669 WO2022096592A1 (fr) 2020-11-06 2021-11-04 Procédé et installation pour produire un ou plusieurs hydrocarbures

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EP4204386A1 true EP4204386A1 (fr) 2023-07-05

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US (1) US20230406786A1 (fr)
EP (1) EP4204386A1 (fr)
CN (1) CN116507600A (fr)
DE (1) DE102020129303A1 (fr)
WO (1) WO2022096592A1 (fr)

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CN104203885A (zh) * 2012-01-31 2014-12-10 巴斯夫欧洲公司 合成气转化成烯烃的方法
AR110129A1 (es) * 2016-11-16 2019-02-27 Dow Global Technologies Llc Procesos y sistemas para obtener alta conversión de carbono a productos deseados en un sistema de catalizador híbrido
EP3587383A1 (fr) 2018-06-21 2020-01-01 Linde Aktiengesellschaft Procédé et système de production d'une ou d'une pluralité de olefins et d'un ou d'une pluralité d'acides carboxyliques

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US20230406786A1 (en) 2023-12-21
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