EP3784381A1 - Réacteur de conversion de réactions réduites à l'équilibre - Google Patents

Réacteur de conversion de réactions réduites à l'équilibre

Info

Publication number
EP3784381A1
EP3784381A1 EP19720485.2A EP19720485A EP3784381A1 EP 3784381 A1 EP3784381 A1 EP 3784381A1 EP 19720485 A EP19720485 A EP 19720485A EP 3784381 A1 EP3784381 A1 EP 3784381A1
Authority
EP
European Patent Office
Prior art keywords
zone
reactor
reactor according
housing
absorbent
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Withdrawn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
EP19720485.2A
Other languages
German (de)
English (en)
Inventor
Manfred Baldauf
Lukas Glöser
Katharina Meltzer
Alexander Tremel
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.)
Siemens AG
Siemens Corp
Original Assignee
Siemens AG
Siemens Corp
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 Siemens AG, Siemens Corp filed Critical Siemens AG
Publication of EP3784381A1 publication Critical patent/EP3784381A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B01J8/009—Membranes, e.g. feeding or removing reactants or products to or from the catalyst bed through a membrane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2475—Membrane reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0207—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal
    • B01J8/0221—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal in a cylindrical shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders

Definitions

  • the invention relates to a reactor for implementing gleichissredu fashioner reactions according to the preamble of Pa tenters 1 and a reactor bundle according to claim 12 and a method for operating a reactor according to claim 13 and a power plant system comprising a power generator and a reactor according to claim 14.
  • Fossil fuels cause carbon dioxide emissions that make it difficult to meet global climate protection goals. For this reason, the expansion of renewable energies is being promoted. However, the generation of renewable electricity is subject to significant regional and temporal fluctuations.
  • the relatively readily available carbon dioxide can thus be used as a cost-effective source of carbon, for example in the production of methanol as a possible product of a co-synthesis of carbon dioxide and hydrogen according to the reaction equation
  • a stirred tank reactor in which an absorbent is present in a lower region of the reactor and reactant gases are passed through a catalyst arrangement, wherein products of the catalyst are widely separated before lying absorbents are added.
  • a catalyst arrangement wherein products of the catalyst are widely separated before lying absorbents are added.
  • the object of the invention is to provide a reactor for the implementation of equilibrium-limited reactions, which can be implemented with less technical outlay compared to the prior art and thereby permit a continuous process which is easily controllable dynamically.
  • Der Reactor according to the invention for the implementation of equilibrium-reduced reactions according to claim 1 comprises a tubular designed reactor housing 4. In this is for the flow of a liquid absorbent arranged a first zone extending in the tube longitudinal direction he stretches. Furthermore, the tubular reactor housing comprises a second zone for receiving a catalyst material, wherein the second zone also extends along the tube longitudinal direction.
  • the invention is characterized in that the first zone and the second zone are separated by a gas-permeable separation zone, wherein the separation zone has a mechanically self-supporting structure. Further, the invention is characterized in that the tubular reactor housing has an aspect ratio greater than six, which means that the length of the tube is at least six times greater than the inner diameter of the tube.
  • the reactor according to the invention allows a continuous flow of absorption liquid in a direct surrounding and along a catalyst material extending along the tubular reactor, so that a product which forms on the catalyst surface can be continuously taken up by the mechanically supporting separation zone alone.
  • the product absorbed by the absorbent product is continuously removed from the reaction zone in the region of the catalyst material, which is why a new product can again arise due to the newly established equilibrium.
  • the reactor according to claim 1 comes almost oh ne moving parts in the reaction, which is why it is subjected to less wear and allows a cost-effective technical structure.
  • the reaction sequence and the degree of conversion can be regulated.
  • tubular is understood here to mean an elongate hollow structure which has an aspect ratio which is greater than six, preferably greater than eight, particularly preferably greater than twelve.
  • the cross section of the tubular reactor housing is round or oval, but other, such as rectangular or square cross-sections are understood to be tubular.
  • the term separating zone is understood to mean a region which has at least one mechanically self-supporting structure which serves, in particular, to separate the catalyst material from the first zone, namely the zone through which the absorbent flows, since the action of the catalyst material has a negative effect on contact with the absorbent would become.
  • the separation zone itself may include several measures taken mechanical and / or chemical nature, for example, they may include hydrophobic layers or spacers Ab hold a mechanically self-supporting network structure or a film structure or a membrane with the cata- tormaterial spaced from the first zone ,
  • the first zone is disposed on an inner wall of the tubular reactor housing.
  • the Absorpti onswashkeit on the reactor housing preferably driven by gravity flow along while reaction products, which are gaseous at ambient conditions, from sorb.
  • the first zone concentrically surrounds the second zone from the inner wall of the tubular reactor.
  • the second zone with the catalyst material is arranged in the center of the tubular reactor and this second zone is surrounded concentrically by the first zone.
  • the term concentric includes in an analogous manner not circular, so also rectangular cross-sections with a. This allows a reactor design that is technically feasible with clotting gem effort.
  • the first zone and the second zone extends along an entire reaction zone of the tubular reactor housing in the tube longitudinal direction and they are along the reaction zone ge separated by the separation zone.
  • This elongated structure with a continuous contact between the first and second zone, only separated by the separation zone allows a particularly continuous course of the reaction and a con- tinuous passage of the absorbent through the Re actuator.
  • the reactor is not verti cal arranged that it has at least an angle of 10 degrees, preferably more, ideally 90 degrees to the vertical. By choosing the angle of inclination of the reactor, the flow rate of the absorbent can be regulated, and thus the reaction itself can be influenced.
  • the first zone of the reactor preferably comprises a porous structure, which in turn preferably has a hydrophilic surface, i. H. in particular has a hydrophilic surface with respect to the absorption liquid.
  • hydrophilic is meant that the wetting angle between the surface and the corresponding liquid is less than 90 degrees.
  • a wetting angle above 90 degrees is hydrophobic.
  • a porous structure with a preferably hydrophilic Oberflä surface allows the slow uniform and targeted fürflie Shen of the absorption liquid through the first zone, which will create as large a surface ge through the porous structure, at which the absorption medium can flow along.
  • the mecha African self-supporting structure of the separation zone is provided with a hydrophobic layer, which in turn causes that liquid absorbent is prevented from entering the second zone penetrate and thus prevented from coming into contact with the Kataly satormaterial.
  • the mechanically self-supporting structure be it in the form of a ceramic medium or in the form of a mesh or a tissue, which is designed to withstand the process temperatures, has a porosity which is greater than the porosity of the porous Structure of the first zone. This allows the products to penetrate the separation zone and subsequent absorption of the products by the absorbent.
  • the reactor comprises an absorbent inlet and an absorbent outlet for continuously passing the Absorpti onsffens through the first zone and includes a Eduktgasein lass for inlet of the educt gas in the second zone.
  • the educt gas preferably remains stationary in the second zone until its complete conversion be available.
  • Such a construction of the second zone is also referred to as dead-end construction.
  • Another component of the invention is a reactor bundle comprising at least two reactors according to one of the preceding claims.
  • the reactor bundle is characterized in that the at least two reactors are arranged together in a coolant reservoir.
  • a further component of the invention is a method for operating a reactor or reactor bundle from the preceding claims, wherein the method is characterized in that an absorbent is continuously introduced into the first zone and discharged at one end of the tubular Re actuator housing again. Further, the gaseous reactant is introduced into the second zone, wherein it is at least partially in egg ner surface of the there, ie in the second zone befindli chen catalyst material in at least a product reacts. The product thus reacted is then led walked walked through the separation zone in the first zone and absorbed by the absorbent and the product is discharged with the absorbent from the reactor.
  • Both the reactor bundle and the method for operating a reactor have the same advantages already set forth with respect to the reactor according to claim 1.
  • the process results in a continuous flow and good controllability of the reaction with little technical outlay. This is also due to a waiver moving mechanical parts due to both the United drive and the reactor bundle.
  • the total benefits described the reactor useful to convert excess energy directly into chemical recyclables is also understood to use the excess energy to produce the educts, for example, for the operation of an electrolyzer for the production of What hydrogen.
  • the methanol reaction already described can preferably be used.
  • the power generation unit is usually a power generator, but it can also serve photovoltaic systems as a power generation unit.
  • a combination of the power generation unit and the reactor in said power plant system is particularly useful when the power plant that includes as the central unit of the power generation unit, energy is generated, which would achieve a low price in the open electricity market.
  • the power plant may be under different shape, it may be a plant for the production of renewable energy, such.
  • B. is a wind turbine, it can also be a classic, especially large fossil power plant, such. B. act a gas power plant.
  • Figure 1 is a schematic representation and detail of a reactor with a tubular housing
  • FIG. 2 shows a reactor bundle from a plurality of reactors according to FIG. 1.
  • FIG. 1 shows a reactor 2 which comprises a tubular reactor housing 4.
  • a first zone 8 is arranged on an inner wall 20 of the reactor housing 4, which serves for the passage of an absorption means (AM) 6.
  • AM absorption means
  • this first zone 8 has a porous structure 18, so that the absorbent 6 comes into contact with egg ner largest possible surface and AS POSSIBLE much absorbent can be passed with a large surface area through the first zone 8.
  • the reactor 2 stands upright, so that the absorbent 6 before due to gravity flows through the first zone 8.
  • the porous structure 18 increases the surface and thus the absorption capacity of the absorbent, but in principle it would also be expedient to allow the absorbent 8 to flow slowly along the inner wall 20 of the reactor housing 4.
  • the absorbent 6 is fed to the upper zone of the reactor in the first zone 8, which is not shown in detail in Figure 1 technically.
  • a second zone 12 in the center of the reactor housing 4 Concentrically surrounded by the first zone 8 is a second zone 12 in the center of the reactor housing 4, wherein in the second zone 12 is substantially a catalyst material 14 is arranged.
  • the catalyst material there are a variety of appropriate options, insbesonde it is a bed, but it can also be porous support material with a high surface flexibilityge provides is applied to the thin-film catalyst material, similar to a catalytic converter from the Au tomobiltechnologie. Cost-effective, however, is a bed of a catalyst material, wherein, for example, a mixture of copper, alumina and zinc oxide is used as a catalyst for methanol production. Grain size and conformity of the poured material are adapted to process technology.
  • a separation zone 16 is between the second zone 12 and the first zone 8 is arranged, which serves in particular to just prevent this contact between rule absorbant 6 and catalyst material 14 to ver.
  • the separation zone 16 is determined in particular by their function, they can contain several components with several different effects to fulfill this function.
  • the separation zone 16 for example, a tissue not shown here, for example, from Me tall, such as stainless steel or carbon or other minera cal fibers contained, in which the catalyst material 14 is held together.
  • One of the essential properties of the separation zone 16 is thus described as comprising a mechanically self-supporting structure 26.
  • the allowstra ing structure 26 is thus fulfilled, for example in the form of a tem peraturbe cleansen and chemically inert tissue. However, it can also be designed in the form of a porous ceramic pot. It is important physical and chemical separation between the absorbent 6 and the catalyst material 14. Furthermore, for example Ab spacers, which are not explicitly shown here, be arranged on the inner wall 20 of the reactor housing 4, which also belong to the separation zone 16 according to this definition, and the self-supporting structure 26, for example, designed in the form of a fabric of the first zone 8 keep away.
  • a gaseous educt 54 which comprises carbon dioxide and hydrogen, in particular in the preparation of methanol, is introduced into the second zone 12 of the reactor 2.
  • alternative educt gases for the implementation of equilibrium-limited reactions are also useful here.
  • the carbon dioxide and hydrogen react on the surface of the catalyst material 14 to methanol, which is gaseous at the prevailing process conditions, for example, 50 bar and 250 degrees Celsius.
  • the (in the process conditions conditions) gaseous product methanol diffuses through the self-supporting structure 26 in the first zone 8 and is absorbed by the absorbent 6.
  • the continuous Lich flowing through the first zone 8 absorbent 6 is discharged from the tube reactor again, wherein the bela dene absorbent is now provided with the reference numeral 6 '.
  • the loaded absorbent 6 ' is discharged in a device, not shown, for example by lowering the pressure and preferably led back to the reaction process.
  • the second zone 12 is preferably at the end of the reactor 2, ie at the lower end to which the loaded from sorbent 6 'is discharged, ge closed for the educt gas.
  • This is also called a dead-end design, which means that the introduced educt gas is forced to react completely to the product, but it is at an educt gas inlet 34 depending on the consumption of the educts 54 continu ously further starting materials 54 introduced.
  • the dead-end design is preferred.
  • There is only a Ven valve 33 is provided to derive a so-called purge gas from the two th zone.
  • the purge gas is undesirable gases, particularly inert gases such as nitrogen, which are produced as waste products during the reaction.
  • the valve 33 is opened at regular intervals during the reaction.
  • the tube longitudinal direction 10 is still to be defined, which takes place ent of the arrow 10 and is characterized by this.
  • a reaction zone 28 which takes place almost over the entire length of the reactor housing 22.
  • FIG. 2 shows a reactor bundle 38, wherein a plurality of reactors 2 are arranged in a coolant reservoir 40 in which a coolant 42 is likewise located.
  • Further Eduktgaszutechnischen 48 and Absorpti onskarzutechnisch 50 are provided, via which the individual Re 2 or reactor housing reactor 4 with reactants 54 be supplied as absorption means 6.
  • the reactors 2 comprise absorbent inlet devices 30, via which the absorbent 6 is conducted into the first zone 8 of the reactor 2.
  • the reactors have a Absorptionsffenauslass 32, in which the laden Absorp tion medium 6 'is discharged and then, not shown here, a product 56 is derived.
  • an inlet 44 is provided for the coolant 42, wherein heat, which is shown schematically in both the figure 1 and in the figure 2 by the reference numeral 58 and which occurs in the reaction in the reactor 2 Re 2, is discharged to the coolant 42 ,
  • the coolant 42 evaporates and is discharged via the coolant outlet 46.
  • This is an isother me process control wherein the temperature present in the reactors, is kept constant by the balance of coolant 42.
  • the resulting water vapor is removed and new coolant 42 is supplied, which contributes to the constant temperature control.
  • a reactor 2 or a reactor bundle 38 is combined with a power generation unit to egg nem power plant system. Due to the fluctuation of the electricity supply in the electricity grids, in particular to the different provision of regenerative
  • the power generation unit in particular a power generator with the described reactor 2 relation ship as the reactor 38.
  • the power plant unit such as a gas power plant or a coal-fired power plant in a constant power spectrum can be operated, which promotes the efficiency of the power plant.
  • the power generation of the power plant does not have to be reduced if the price of electricity is low, but the energy can be introduced into the reactor bundle 38, for example, in the described chemical reaction or in the reactor 2.
  • carbon dioxide which is essential in the combustion of fossil fuels. Weigerlich arises branch off from the exhaust gases of the power plant and sen in the process for the production of Wertga, as described, feed in the synthesis of methanol as a reactant gas carbon dioxide.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un réacteur de conversion de réactions réduites à l'équilibre comprenant un boîtier de réacteur (4) réalisé sous forme de tube - dans lequel est agencée une première zone (8) servant au passage d'un moyen d'absorption (6) liquide qui s'étend dans la direction longitudinale du tube (10) et - dans lequel une deuxième zone (12) s'étendant également dans la direction longitudinale du tube (10) pour l'accueil d'un matériau de catalyseur (14) étant agencé. L'invention se caractérise - en ce que la première zone (8) et la deuxième zone (12) sont séparées par une zone séparatrice (16) perméable aux gaz, - en ce que la zone séparatrice (16) comporte une structure autoporteuse (26) mécanique et - en ce que le rapport d'aspect du boîtier de réacteur (4) tubulaire le long de la zone de réaction (28) est supérieur à 6.
EP19720485.2A 2018-04-20 2019-04-17 Réacteur de conversion de réactions réduites à l'équilibre Withdrawn EP3784381A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP18168501.7A EP3556460A1 (fr) 2018-04-20 2018-04-20 Réacteur de mise en uvre de réactions à équilibre réduit
PCT/EP2019/059882 WO2019201974A1 (fr) 2018-04-20 2019-04-17 Réacteur de conversion de réactions réduites à l'équilibre

Publications (1)

Publication Number Publication Date
EP3784381A1 true EP3784381A1 (fr) 2021-03-03

Family

ID=62046680

Family Applications (2)

Application Number Title Priority Date Filing Date
EP18168501.7A Withdrawn EP3556460A1 (fr) 2018-04-20 2018-04-20 Réacteur de mise en uvre de réactions à équilibre réduit
EP19720485.2A Withdrawn EP3784381A1 (fr) 2018-04-20 2019-04-17 Réacteur de conversion de réactions réduites à l'équilibre

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP18168501.7A Withdrawn EP3556460A1 (fr) 2018-04-20 2018-04-20 Réacteur de mise en uvre de réactions à équilibre réduit

Country Status (6)

Country Link
US (1) US20210154634A1 (fr)
EP (2) EP3556460A1 (fr)
CN (1) CN112004594A (fr)
CL (1) CL2020002702A1 (fr)
MA (1) MA51536B1 (fr)
WO (1) WO2019201974A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP7719082B2 (ja) * 2020-08-31 2025-08-05 住友化学株式会社 化学反応方法、化学反応装置および製造方法
CN113041970B (zh) * 2021-03-17 2021-11-26 南京理工大学 一种内置扰流结构催化膜式反应器
EP4480575A1 (fr) * 2023-06-23 2024-12-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Réacteur refroidi pour effectuer des réactions exothermes équilibrées

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS585691B2 (ja) * 1978-09-27 1983-02-01 理化学研究所 多段交換反応塔
JP2001342155A (ja) * 2000-06-01 2001-12-11 Nkk Corp スラリー床反応器
US20070264190A1 (en) * 2006-05-09 2007-11-15 Qinglin Zhang Fixed-bed reactors and catalytic processes
AR066573A1 (es) * 2007-05-18 2009-08-26 Shell Int Research Un sistema reactor un absorbente y un proceso para la reaccion de una fuente
GB201000156D0 (en) * 2010-01-07 2010-02-24 Gas2 Ltd Isothermal reactor for partial oxidisation of methane
GB201107072D0 (en) * 2011-04-27 2011-06-08 Davy Process Techn Ltd Process
CN102584526B (zh) * 2011-12-28 2014-09-10 上海碧科清洁能源技术有限公司 一种由合成气制备甲醇的膜接触器方法以及用于该方法的膜反应器
DE102016204717A1 (de) * 2016-03-22 2017-09-28 Siemens Aktiengesellschaft Reaktor zur Durchführung von gleichgewichtslimitierten Reaktionen
DE102016210224A1 (de) 2016-06-09 2017-12-14 Friedrich-Alexander-Universität Erlangen-Nürnberg Reaktor und Verfahren zur Umsetzung von gleichgewichtslimitierten Reaktionen
JP7049075B2 (ja) * 2016-07-04 2022-04-06 公益財団法人地球環境産業技術研究機構 メタノール製造方法およびメタノール製造装置

Also Published As

Publication number Publication date
CN112004594A (zh) 2020-11-27
EP3556460A1 (fr) 2019-10-23
US20210154634A1 (en) 2021-05-27
CL2020002702A1 (es) 2021-04-05
MA51536A1 (fr) 2021-04-30
MA51536B1 (fr) 2022-11-30
WO2019201974A1 (fr) 2019-10-24

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