DE102015202681A1 - Process for carrying out a chemical synthesis - Google Patents
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- DE102015202681A1 DE102015202681A1 DE102015202681.7A DE102015202681A DE102015202681A1 DE 102015202681 A1 DE102015202681 A1 DE 102015202681A1 DE 102015202681 A DE102015202681 A DE 102015202681A DE 102015202681 A1 DE102015202681 A1 DE 102015202681A1
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- 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
- C07C29/1512—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 reaction conditions
- C07C29/1514—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 reaction conditions the solvents being characteristic
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
- B01D17/02—Separation of non-miscible liquids
- B01D17/0205—Separation of non-miscible liquids by gas bubbles or moving solids
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- 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
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1868—Stationary reactors having moving elements inside resulting in a loop-type movement
- B01J19/1881—Stationary reactors having moving elements inside resulting in a loop-type movement externally, i.e. the mixture leaving the vessel and subsequently re-entering it
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- 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
- B01J8/005—Separating solid material from the gas/liquid stream
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- 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
- B01J8/0242—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 vertical
- B01J8/025—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 vertical in a cylindrical shaped bed
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- 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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
- B01J8/224—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement
- B01J8/228—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement externally, i.e. the particles leaving the vessel and subsequently re-entering it
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- 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
- B01J2208/00176—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles outside the reactor
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- 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
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00283—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant liquids
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- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00042—Features relating to reactants and process fluids
- B01J2219/00047—Ionic liquids
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- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00103—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor in a heat exchanger separate from the reactor
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- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
- B01J2219/0011—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling involving reactant liquids
Abstract
Die Erfindung betrifft ein Verfahren zur Durchführung einer chemischen Synthese unter Verwendung von zwei nur teilweise ineinander löslichen Trägerphasen und einem Katalysator, der in einer der Trägerphasen dispergiert vorliegt, umfassend folgende Schritte: Vermischen der Trägerphasen in einem Reaktor, Einleiten mindestens eines Syntheseeduktes in den Reaktor und Trennung der beiden Trägerphasen.The invention relates to a method for carrying out a chemical synthesis using two only partially mutually soluble carrier phases and a catalyst which is dispersed in one of the carrier phases, comprising the following steps: mixing the carrier phases in a reactor, introducing at least one synthesis product into the reactor and Separation of the two carrier phases.
Description
Der Umsatz bei chemischen Reaktionen ist durch die Gleichgewichtslage der Reaktion beschränkt. Liegt das chemische Gleichgewicht einer Synthesereaktion nur teilweise auf der Seite der Produkte, führt eine einstufige Reaktionsführung nur zu einem Teilumsatz. Es wird daher nur ein Teil der Edukte bei einem Durchgang durch den Reaktor umgesetzt. Das technische Problem der Erfindung ist daher die Erhöhung des Umsatzes von gleichgewichtslimitierten Reaktionen bei einem einfachen Durchgang durch einen Synthesereaktor. The conversion in chemical reactions is limited by the equilibrium position of the reaction. If the chemical equilibrium of a synthesis reaction is only partially on the side of the products, a one-step reaction procedure only leads to a partial conversion. Therefore, only a portion of the starting materials is reacted in one pass through the reactor. The technical problem of the invention is therefore to increase the turnover of equilibrium-limited reactions in a single pass through a synthesis reactor.
Sehr viele Reaktionen sind gleichgewichtslimitiert. Bei der chemischen Synthese sind dies z.B. die Erzeugung von Methanol aus Wasserstoff und Kohlenstoffmonoxid und oder Kohlenstoffdioxid, oder die Erzeugung von Ammoniak aus Wasser und Stickstoff. Diese Reaktionen finden heute in heterogenen katalysierten Festbett- oder Slurryreaktoren statt. Die Edukte werden bei einem einfachen Durchgang durch den Reaktor nur teilweise umgesetzt. Danach werden üblicherweise die Reaktionsprodukte abgetrennt und die nicht umgesetzten Edukte werden zum Reaktionseintritt rezirkuliert. Die Rezirkulation von teils großen Gasmengen führt zu einem hohen apparativen Aufwand. Der Druckverlust im Reaktor muss durch eine Rezirkulationseinheit ausgeglichen werden. Diese wird meist bei hohen Temperaturen betrieben und führt zu hohen Kosten. Zudem reichern sich durch die Rezirkulation Inert- und Fremdgase im Kreislauf an, was zu negativen Einflüssen auf die Reaktionsführung führt. Bei Rezirkulation wird daher kontinuierlich eine kleine Menge an Rezirkulationsgas abgezogen, was Verluste an Edukten und damit niedrigere Umsetzungswirkungsgrade zur Folge hat. Weiterhin führt die zurückgeführte Gasmenge zu einem hohen Gasvolumenstrom durch den Reaktor, was die Baugröße und damit die Kosten des Reaktors erhöht. Very many reactions are equilibrium-limited. In chemical synthesis, these are e.g. the production of methanol from hydrogen and carbon monoxide and / or carbon dioxide, or the production of ammonia from water and nitrogen. These reactions take place today in heterogeneous catalyzed fixed bed or slurry reactors. The reactants are only partially reacted in a simple passage through the reactor. Thereafter, the reaction products are usually separated and the unreacted starting materials are recirculated to the reaction. The recirculation of some large amounts of gas leads to a high expenditure on equipment. The pressure drop in the reactor must be compensated by a recirculation unit. This is usually operated at high temperatures and leads to high costs. In addition, due to recirculation inert and foreign gases accumulate in the circulation, which leads to negative effects on the reaction. With recirculation, therefore, a small amount of recirculation gas is continuously withdrawn, which results in losses of starting materials and thus lower conversion efficiencies. Furthermore, the recirculated amount of gas leads to a high volume of gas flow through the reactor, which increases the size and thus the cost of the reactor.
Der Erfindung liegt daher die Aufgabe zugrunde, ein Verfahren zur Durchführung einer chemischen Synthese bereitzustellen, bei dem gegenüber dem Stand der Technik bei gleichem oder verringertem Energieaufwand ein höherer Umsetzungsgrad der Edukte erzielbar ist. The invention is therefore based on the object to provide a method for carrying out a chemical synthesis in which over the prior art with the same or reduced energy consumption, a higher degree of conversion of the reactants can be achieved.
Die Lösung der Aufgabe besteht in einem Verfahren zur Durchführung einer chemischen Synthese mit den Merkmalen des Patentanspruchs 1. The solution of the problem consists in a method for carrying out a chemical synthesis with the features of claim 1.
Das erfindungsgemäße Verfahren zur Durchführung einer chemischen Synthese erfolgt unter Verwendung von zwei nur teilweise ineinander löslichen Trägerphasen und einem Katalysator, der in einer der Trägerphasen dispergiert vorliegt. Im Idealfall sind die beiden Trägerphasen überhaupt nicht ineinander lösbar. Da dies thermodynamisch jedoch nicht umsetzbar ist, und selbst bei einer sehr schlechten Benetzung stets eine Restlöslichkeit durch Diffusion vorhanden ist, werden Trägerphasen herangezogen, die möglichst wenig, also nur teilweise, ineinander lösbar sind. Auch der Katalysator liegt real betrachtet stets in beiden Phasen vor, es ist jedoch zweckmäßig so, dass der Katalysator zum möglichst großen Teil in einer der beiden Phasen vorliegt. The inventive method for carrying out a chemical synthesis is carried out using two only partially mutually soluble carrier phases and a catalyst which is dispersed in one of the carrier phases. Ideally, the two carrier phases are not at all dissolvable. Since this is thermodynamically not feasible, and even with a very poor wetting always a residual solubility by diffusion is present, carrier phases are used, which are as little as possible, so only partially, are dissolvable. The catalyst is always present in both phases in real terms, but it is expedient that the catalyst is present for the most part in one of the two phases.
Das Verfahren umfasst folgende Schritte:
Zunächst erfolgt ein Vermischen der Trägerphasen in einem Reaktor. In diesem Reaktor wird zudem mindestens ein, in der Regel mehrere Syntheseedukte eingeleitet, wonach schließlich eine Trennung der beiden Trägerphasen erfolgt. The method comprises the following steps:
First, the carrier phases are mixed in a reactor. In addition, at least one, generally several synthesis educts are introduced into this reactor, after which finally a separation of the two carrier phases takes place.
Nach Einleiten des mindestens einen Syntheseeduktes in den Reaktor, erfolgt eine Reaktion der Edukte zu Syntheseprodukten, insbesondere an der Katalysatoroberfläche wobei die Reaktion zu den Produkten hin bei Erreichen des thermodynamischen Gleichgewichtes an der Katalysatoroberfläche zum Stillstand kommt. Würde nur eine Trägerphase vorliegen, in der der Katalysator dispergiert vorliegt, käme die Reaktion nun zum Erliegen. Durch die Zweiphasigkeit der möglichst nicht ineinander gelösten Trägerphasen ist es nun jedoch so, dass die Syntheseprodukte sich von der einen Phase bevorzugt in die andere Phase bewegen, um dort einen Konzentrationsausgleich zu erschaffen um maximal die Sättigungskonzentration in jeder Phase zu erreichen, was eine Anreicherung der Syntheseprodukte in der zweiten Trägerphase bewirkt, da diese bevorzugt eine höhere Aufnahmefähigkeit für die Produkte besitzt. Ferner bewirkt dies, dass die Gleichgewichtslimitierung an der Katalysatoroberfläche nicht mehr beschränkend ist und die chemische Reaktion insoweit weiter stattfindet, da das Einstellen einer stationären Gleichgewichtssituation verhindert wird. Hierbei werden wiederum kontinuierlich die Produkte von der Katalysatoroberfläche abgeführt und in der zweiten Trägerphase angereichert. Der Umsetzungsgrad der Edukte zu den Produkten ist somit höher als dies durch das thermodynamische Gleichgewicht zwischen Syntheseedukten und Syntheseprodukten der Fall wäre. After introduction of the at least one synthesis educt into the reactor, a reaction of the reactants to synthesis products, in particular at the catalyst surface, whereby the reaction to the products comes to a standstill upon reaching the thermodynamic equilibrium at the catalyst surface. If only one carrier phase were present in which the catalyst is dispersed, the reaction would now stop. However, due to the two-phase nature of the carrier phases, which are as far as possible incapable of each other, the synthesis products preferably move from one phase into the other phase in order to create a concentration balance there in order to achieve a maximum of the saturation concentration in each phase, which results in an enrichment of the Synthesis products in the second carrier phase causes, since this preferably has a higher capacity for the products. Further, this causes the equilibrium limitation at the catalyst surface to be no longer restrictive and the chemical reaction continues to occur insofar as the setting of a stationary equilibrium situation is prevented. Here again the products are continuously removed from the catalyst surface and enriched in the second carrier phase. The degree of conversion of the starting materials to the products is thus higher than would be the case by the thermodynamic equilibrium between synthesis and synthesis products.
In einem weiteren Prozessschritt werden nun die beiden Trägerphasen voneinander getrennt. Sollte die zweite Trägerphase, die das angereicherte Syntheseprodukt umfasst mit diesem zusammen bereits einen Wertstoff bilden, so kann auf eine Abtrennung des Syntheseproduktes aus der zweiten Trägerphase verzichtet werden. Sollte dies nicht der Fall sein, so kann in einem weiteren Verfahrensschritt das Syntheseprodukt aus einer der beiden, hier der zweiten Trägerphase, abgetrennt werden. In a further process step, the two carrier phases are now separated from each other. Should the second carrier phase, which comprises the enriched synthesis product, already form a valuable substance together with it, separation of the synthesis product from the second carrier phase can be dispensed with. If this is not the case, then in a further process step, the synthesis product can be separated from one of the two, here the second carrier phase.
Bei der Art der Trägerphasen kann es zweckmäßig sein, dass es sich um eine Flüssigkeit- und eine Gasphase oder insbesondere bevorzugt um zwei Flüssigkeiten handelt. Hierbei ist es wiederum zweckmäßig, wenn eine der beiden Flüssigkeiten polare Eigenschaften aufweist, und die andere Flüssigkeit unpolare Eigenschaften. Für bestimmte Reaktionssysteme (z.B. Methanol-Synthese) hat sich herausgestellt, dass Syntheseprodukte (z.B. Methanol, Wasser) eine Affinität zu polaren Flüssigkeiten aufweisen und sich in diesen anreichern. Ferner ist es zweckmäßig, wenn der Katalysator dann bevorzugt, d. h. mindestens zu 60% in der unpolaren Flüssigkeit vorliegt. Die Edukte der Reaktionen befinden sich dann in beiden Phasen gelöst. In diesem Fall findet die Synthesereaktion bevorzugt auf der Oberfläche des Katalysators in der unpolaren Flüssigkeit statt, die Syntheseprodukte reichern sich allerdings in der polaren Flüssigkeit an. In the type of carrier phases, it may be appropriate that it is a liquid and a gas phase or more preferably two liquids. In this case, it is again expedient if one of the two liquids has polar properties, and the other liquid has nonpolar properties. For certain reaction systems (eg methanol synthesis) it has been found that synthesis products (eg methanol, water) have an affinity to polar liquids and accumulate in them. Furthermore, it is expedient if the catalyst is then preferred, ie at least 60% present in the non-polar liquid. The educts of the reactions are then dissolved in both phases. In this case, the synthesis reaction preferably takes place on the surface of the catalyst in the non-polar liquid, but the synthesis products accumulate in the polar liquid.
Als polare Flüssigkeiten haben sich insbesondere Wasser (nur wenn Wasser kein Syntheseprodukt ist), aber auch ionische Flüssigkeiten, polare Lösungsmittel oder höhermolekulare Alkohole als zweckmäßig herausgestellt. Im Gegenzug dazu werden als unpolare Flüssigkeiten insbesondere Öle wie z.B. Wärmeträgeröle wie Witco, Marlotherm oder Dowtherm A verwendet. As polar liquids, in particular water (only if water is not a synthesis product), but also ionic liquids, polar solvents or higher molecular weight alcohols have been found to be expedient. In return, nonpolar liquids, in particular oils such as e.g. Heat transfer oils such as Witco, Marlotherm or Dowtherm A are used.
In einer weiteren Ausgestaltungsform der Erfindung werden die beiden Trägerphasen außerhalb des Reaktors in einem Absetzbecken voneinander getrennt. Dies ermöglicht einen kontinuierlichen Prozess, so dass während der Absetzzeit aufgrund eines Dichteunterschieds zwischen den Phasen und des Trennvorganges zwischen den beiden Trägerphasen die Reaktion im Reaktor durch Wiederbefüllen dieses mit den Trägerphasen und Edukten weiter erfolgen kann. In a further embodiment of the invention, the two carrier phases are separated from one another outside the reactor in a settling tank. This allows a continuous process, so that during the settling time due to a density difference between the phases and the separation process between the two carrier phases, the reaction in the reactor can be carried out by refilling this with the carrier phases and educts on.
Vorteilhafte Ausgestaltungsformen der Erfindung sowie weitere Merkmale werden anhand der folgenden Figur näher erläutert. Dabei handelt es sich um eine rein schematische Darstellung, die somit keine Einschränkung des Schutzbereichs darstellt. Advantageous embodiments of the invention and further features will be explained in more detail with reference to the following figure. This is a purely schematic representation, which thus does not represent a limitation of the scope.
Die einzige Figur zeigt:
Eine schematische Darstellung eines Syntheseverfahrens mit einem Reaktor und einem Absetzbecken. The only figure shows:
A schematic representation of a synthesis process with a reactor and a settling tank.
In der Figur ist eine schematische Darstellung des zu beschreibenden Reaktionskonzeptes gegeben. Hierzu kommt zunächst ein Reaktor
Als Trägerphasen
Die verwendeten Trägerphasen
Im Weiteren werden die gasförmigen und/oder flüssigen Edukte
Im Weiteren wird nun das Gemisch der beiden Trägerphasen
In diesem Fall, in dem Wasserstoff mit Kohlenmonoxid bzw. Kohlendioxid zu Methanol und Wasser (bei Verwendung von CO2) reagiert wird, wird das Reaktionsprodukt
Bisher wurde das Reaktionskonzept so beschrieben, dass sich der Katalysator bevorzugt in der unpolaren Flüssigkeit
Die Reaktionsbedingungen des Reaktors
Die Wärme, die dem Reaktor
Claims (10)
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DE102015202681.7A DE102015202681A1 (en) | 2015-02-13 | 2015-02-13 | Process for carrying out a chemical synthesis |
PCT/EP2016/051049 WO2016128188A1 (en) | 2015-02-13 | 2016-01-20 | Method for carrying out a chemical synthesis |
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102017204226A1 (en) | 2017-03-14 | 2018-09-20 | Friedrich-Alexander-Universität Erlangen-Nürnberg | Mixture for use as a liquid sorbent in methanol synthesis and method for methanol synthesis using the mixture |
EP3492165A1 (en) | 2017-11-29 | 2019-06-05 | Siemens Aktiengesellschaft | Reactor complex for implementing equal weight limited reactions and method for same |
EP4059596A1 (en) * | 2021-03-16 | 2022-09-21 | Paul Scherrer Institut | Process for methanol production from co2 with water removal |
Families Citing this family (2)
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DE102016204719A1 (en) * | 2016-03-22 | 2017-09-28 | Siemens Aktiengesellschaft | reactor |
EP3556451B1 (en) * | 2018-04-20 | 2020-06-03 | Siemens Aktiengesellschaft | Method for operating a reactor system |
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DE69816855T2 (en) * | 1997-10-06 | 2004-04-22 | Catalytic Distillation Technologies, Pasadena | METHOD FOR CARRYING OUT HETEROGENEOUS CATALYSIS |
DE102010002202A1 (en) * | 2010-02-22 | 2011-08-25 | Wacker Chemie AG, 81737 | Process for the preparation of ester-functional silanes |
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NL1003026C2 (en) * | 1996-05-03 | 1997-11-06 | Tno | Reactor for conducting gas phase / liquid phase / solid phase reactions, as well as a method for conducting such reactions using this reactor. |
JP2009535497A (en) * | 2006-04-12 | 2009-10-01 | ナノマス テクノロジーズ インコーポレイテッド | Nanoparticles, method for producing the same, and use thereof |
EP2354131A1 (en) * | 2010-02-02 | 2011-08-10 | Momentive Specialty Chemicals Research Belgium | Process for the manufacture of a 1,2-epoxide and a device for carrying out said process |
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2015
- 2015-02-13 DE DE102015202681.7A patent/DE102015202681A1/en not_active Withdrawn
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2016
- 2016-01-20 WO PCT/EP2016/051049 patent/WO2016128188A1/en active Application Filing
Patent Citations (3)
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