EP3016924A1 - Procédé et système de réacteur de synthèse de méthanol avec recyclage du gaz circulant et du gaz de purge - Google Patents

Procédé et système de réacteur de synthèse de méthanol avec recyclage du gaz circulant et du gaz de purge

Info

Publication number
EP3016924A1
EP3016924A1 EP13721306.2A EP13721306A EP3016924A1 EP 3016924 A1 EP3016924 A1 EP 3016924A1 EP 13721306 A EP13721306 A EP 13721306A EP 3016924 A1 EP3016924 A1 EP 3016924A1
Authority
EP
European Patent Office
Prior art keywords
gas
reactor
methanol
content
carbon dioxide
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Withdrawn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
EP13721306.2A
Other languages
German (de)
English (en)
Inventor
Lothar Brehm
Hermann Göhna
Peter König
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.)
Silicon Fire AG
Original Assignee
Silicon Fire AG
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 Silicon Fire AG filed Critical Silicon Fire AG
Publication of EP3016924A1 publication Critical patent/EP3016924A1/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Withdrawn legal-status Critical Current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
    • B01J8/001—Controlling catalytic processes
    • 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
    • B01J8/0278—Feeding reactive fluids
    • 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
    • B01J8/1809—Controlling processes
    • 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
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • 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
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • 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
    • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
    • 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
    • B01J2208/00539—Pressure
    • 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
    • B01J2208/00601—Controlling the conductivity
    • 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
    • B01J2208/00628—Controlling the composition of the reactive mixture
    • 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
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00946—Features relating to the reactants or products
    • B01J2208/00955—Sampling of the particulate material, the reactants or the products
    • B01J2208/00964—Reactants
    • 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
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
    • 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
    • B01J2219/00191—Control algorithm
    • B01J2219/00193—Sensing a parameter
    • B01J2219/00195—Sensing a parameter of the reaction system
    • B01J2219/00198—Sensing a parameter of the reaction system at the reactor inlet
    • 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
    • B01J2219/00191—Control algorithm
    • B01J2219/00211—Control algorithm comparing a sensed parameter with a pre-set value
    • B01J2219/00213—Fixed parameter value
    • 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
    • B01J2219/00191—Control algorithm
    • B01J2219/00222—Control algorithm taking actions
    • B01J2219/00227—Control algorithm taking actions modifying the operating conditions
    • B01J2219/00229—Control algorithm taking actions modifying the operating conditions of the reaction system
    • B01J2219/00231—Control algorithm taking actions modifying the operating conditions of the reaction system at the reactor inlet

Definitions

  • the present application relates to methods and reactor systems for providing methanol.
  • it is about the catalytic
  • Carbon dioxide C0 2 (usually called carbon dioxide) is a compound that is a compound that has a wide range of carbon dioxide.
  • Carbon dioxide is a colorless and odorless gas. It is a natural component of the air with a low concentration and is formed in living beings in cell respiration, but also in the combustion of carbonaceous substances with sufficient
  • climate neutrality is sought by pursuing approaches that attempt to compensate for the associated with C0 2 emissions energy production in one place by generating alternative energy in other places. This approach is strong
  • FIG. 1 Issuers of greenhouse gases (GHG), such as industrial companies (eg car manufacturers) 1 or power plant operators 2, invest or operate eg. For example, wind farms 3 at other locations in the context of balancing projects in order to generate energy without GHG emissions. In purely mathematical terms, this can result in climate neutrality. Numerous companies are trying to buy a "climate-neutral vest" in this way.
  • GHG greenhouse gases
  • Such a combination makes it possible to produce hydrocarbon-based energy sources in corresponding silicone-fire plants.
  • These silicon-fire systems are particularly suitable for synthesizing methanol.
  • This system is characterized by a particularly favorable
  • Circular gas ratio (P / E) and therefore has numerous environmental and economic advantages over other known reactors for
  • a reactor system for providing a methanol-containing product is provided.
  • a method for using or operating such a reactor plant is proposed.
  • a carbon-containing gas fraction preferably carbon dioxide
  • the carbon-containing gas fraction is reacted with a hydrogen portion in the presence of a synthesis reaction catalyst to convert these gases to the methanol-containing product.
  • C0 2 separation is removed from a combustion process or an oxidation process of carbon or hydrocarbons by C0 2 separation.
  • C0 2 but z. B. also come from a sewage treatment plant, a biogas plant or a separation stage, which separates the C0 2 share of naturally occurring raw gas.
  • C0 2 can be provided, for example, via a longer pipeline, a local gas line or even in steel cylinders or tanks.
  • the hydrogen can over a longer pipeline, a local
  • the hydrogen is produced locally by means of electrolysis of water or provided by a sewage treatment plant or a biogas plant.
  • the hydrogen may also be generated by an oxidation reaction of elemental silicon or other elemental metal.
  • Carbon dioxide as a carbon source can be removed according to the invention also from raw gas, which depending on the natural gas source about 10%
  • Carbon dioxide can z. B. also originate from processes of Kalkbumpss or calcination to soda.
  • the invention is used in a reactor plant or for use, which is designed specifically for the synthesis of a methanol-containing product.
  • the synthesis is carried out using a starting material containing a gas Carbon content (preferably carbon dioxide) and hydrogen content.
  • the reactor of the reactor plant has a gas inlet and a
  • Product gas outlet wherein a process stage is arranged at the product gas outlet. This process stage is designed to produce a product gas mixture that is at the
  • Product gas outlet is provided, in a purge gas, in a
  • the reactor system further comprises a cycle gas recirculation to lead back the cycle gas fraction and combine with the starting material before the resulting mixed gas can be fed to the gas inlet.
  • the mixture of the starting materials has process-related to a hydrogen excess. This excess must be removed from the process (eg by blowing off) to maintain process pressure.
  • the surplus, which is blown off, is called purge gas (exhaust gas) and is flared so far mainly in large plants, underfeuert and in very small systems of small quantities due to the environment
  • the reactor system of the invention is characterized in that it comprises a return line, the so with its line input to the downstream process stage and with its line output with a
  • the reactor plant therefore according to the invention comprises a measuring device which is arranged in the region of the input stage for determining the instantaneous carbon dioxide fraction.
  • control means which are arranged in the region of the input stage for predetermining the carbon dioxide proportion and / or the hydrogen content.
  • the process control in the reactor plant is such that the
  • Purgegas a carbon dioxide content, a hydrogen content and a
  • the control means together with the measuring device are able to compensate for these process fluctuations by regulating the fresh carbon dioxide content and / or the fresh hydrogen content on the input side of the input stage.
  • the measuring device In order to control the process fluctuations control, the measuring device must be able to determine the carbon dioxide content in the gas flow of the return line quickly and reliably.
  • the invention is here in preferred embodiments to a
  • Carbon content carbon dioxide and carbon monoxide together
  • the hydrogen content can be reliably determined and distinguished from the hydrogen content, such as
  • the thermal conductivity sensor directly determines the thermal conductivity of the purge gas, taking advantage of the fact that for a given temperature, gas molecules have the same mean kinetic energy. That Carbon dioxide and hydrogen of the gas stream have the same mean kinetic energy (e.g., at one
  • a hydrogen atom with the relative mass 1 has a much greater velocity than the carbon dioxide with the relative mass 44. Because of this higher molecular velocity, hydrogen transports energy faster than carbon dioxide, that is, the thermal conductivity is greater.
  • the thermal conductivity of carbon dioxide is more than 10 times lower than the thermal conductivity of hydrogen. This difference becomes one in preferred embodiments Thermal conductivity sensor determined.
  • the inventive recirculation design for the purge gas is characterized in that a simple, robust and fast control is provided, the
  • volume control of the feed gases H 2 and C0 2 provides.
  • the so-called solvent gas can be recycled in order to achieve a further improvement.
  • the reactor system according to the invention is controlled and the individual processes are "linked" with each other so that
  • Reactor plant to be as minimal as possible.
  • regenerative electrical energy is used to operate the reactor system in all embodiments.
  • methanol is produced as a storable and transportable energy form. That is, renewable energy is chemically transformed into an uncritical and relatively simple storage and transportable (liquid) form of energy.
  • Methanol can serve as an energy buffer.
  • methanol can be stored in order to be able to provide additional electrical energy in the event of peak energy demand in the electrical grid.
  • methanol can either be incinerated in thermal power plants, or electric energy can be generated in fuel cells (eg direct methanol fuel cells, MFC).
  • the methanol can be catalytically converted into a cracking gas of hydrogen and carbon monoxide before combustion. This results in advantages in certain implementation processes.
  • Preferred embodiments of the invention are based on the hydrogen production by means of electrical energy, which is generated as far as possible renewable and comes for example from wind, water and / or solar power plants.
  • Hydrogen, the z. B. produced by electrolysis or by the use of elemental silicon and water, so does not need stored or highly compressed or liquefied refrigerated and transported over long distances, but serves as an intermediate, preferably at the location of its production directly the the aforementioned reaction for the production of methanol is supplied.
  • an energy-converting process in which regenerative energy is converted into electrical energy is followed, for example, by material-converting (chemical) processes, namely the intermediary provision of hydrogen and the conversion of the hydrogen together with a carbon carrier (here in the form of Carbon dioxide) to methanol.
  • material-converting (chemical) processes namely the intermediary provision of hydrogen and the conversion of the hydrogen together with a carbon carrier (here in the form of Carbon dioxide) to methanol.
  • FIG. 1 shows a diagram representing the basic steps of the method according to the invention, or a corresponding Silicon-Fire plant;
  • FIG. 1 shows a side elevational view of an exemplary reactor of the invention
  • Fig. 3 shows a schematic view of a reactor plant of the invention, e.g. a reactor according to FIG. 4 can be used;
  • FIG. 4 shows a schematic view of the high-pressure region of another reactor plant according to the invention, wherein z. B. a reactor of FIG. 4 can be used.
  • energy source is used here for liquids that z. B. can be used as fuel or fuel. This refers in particular to methanol 108 or to products containing methanol 108.
  • methanol-containing product is used here because the product which is provided at the outlet 201 of a reactor system 50 does not consist of one hundred percent methanol rather, a so-called
  • methanol-containing product 108 physical mixture of methanol and water, referred to herein as methanol-containing product 108.
  • methanol-containing product 108 By a subsequent distillation process can then be recovered if necessary pure methanol.
  • the process direction the direction from the input side E to the output side A, i. the flow or flow direction SR in the interior of a reactor 10 and the reactor system 50 is designated. Details are shown in FIG. 5.
  • the pressure range between 1 bar and 30 bar is referred to here.
  • the pressure range between 50 bar and 100 bar is referred to here.
  • the reactor plant 50 of the invention as shown in FIG. 5 and 6 are shown by way of example, e.g. the input side of static mixer 257 (i.e., supply line 258 to static mixer 257) in said low pressure region.
  • the return line 250 is in the low pressure region, if the return line 250 couples the purge gas PG before the static mixer 257.
  • the gas inlet 21, the reactor 10, the gas outlet 23 and the recycle gas 262, however, are in the aforementioned high-pressure area.
  • a passive mixing element is referred to the gases with respect to temperature and / or concentration
  • As (gas) compressor (eg, the compressors 260, 263) is here called a compressor that compresses gases, ie, the pressure of the gas increases when flowing from the input side of the (gas) compressor to the output side.
  • gases gases are in process engineering well known.
  • a heater / heat exchanger 267 here an element or an assembly is referred to the / can heat or cool the gas stream as needed. Since the heater / heat exchanger 267 is used in the high-pressure region of the reactor system 50, a high-pressure heater / heat exchanger 267 is used.
  • Such heaters / heat exchangers 267 are well known in the process engineering.
  • the / a high pressure gas cooling down As a final cooler 269 here an element or an assembly is referred to, the / a high pressure gas cooling down. In all embodiments, this is preferably a high-pressure gas cooler. In the figures, it is schematically indicated that the end cooler 269 a
  • Cooling loop 286 includes. This cooling loop 286 may be e.g. be passed through water to escape the high-pressure gas process heat. Such high pressure gas coolers are well known in the process engineering.
  • a high-pressure separator 270 an element is referred to here, which receives a product gas mixture PGG and separates into gas and liquid. The gas is released either via the output 274 as a recycle gas KG or via the output 277 as purge gas PG.
  • a level gauge 272 together with an actuator S4 form a level control that controls this operation as needed. This level control maintains the liquid level at a predetermined level in the high pressure separator 270.
  • the high pressure separator 270 and the liquid level are sized to provide sufficient time to blow off / discharge the crude methanol while leaving no foam or mist on the gas side.
  • the level control is preferably autonomous in all embodiments and does not control any other operation in the reactor plant 50.
  • the purge gas PG is discharged as surplus at the pressure hold controller 280 / S6.
  • peripheral equipment parts 272, S4, 280, S6 are in process engineering
  • a low-pressure separator 271 here an element is referred to, which receives a liquid and separates C0 2 gas from this liquid.
  • the C0 2 gas is released via the outlet 278 as the release gas LG.
  • Low-pressure separator 271 and also the peripheral system parts 273, S5 are well known in the process engineering.
  • synthesis reactor 10 Another element of the methanol synthesis is the synthesis reactor 10. Details of a suitable reactor 10 are the above-mentioned international patent application PCT / EP2010 / 064948 of the present
  • Fig. 2 shows a schematic block diagram of the
  • This overall plant 100 is designed so that a method of providing the methanol-containing product 108 can be carried out.
  • the corresponding procedure is based on the following basic steps.
  • carbon dioxide 101 is provided as a carbon source and hydrogen 103.
  • the required for providing the hydrogen 103 DC electric energy El is here as far as possible generated by means of renewable energy technology and the entire system 100 is provided.
  • Particularly suitable as renewable energy technology are solar thermal systems 300 and photovoltaic systems 400, which are based on solar modules.
  • hydropower can also be used.
  • Water electrolysis 105 is used as shown in FIG DC electric power El performed to produce the hydrogen (gas) 103 as an intermediate of water 102.
  • FIG. 2 an overall system 100 is shown.
  • an economically and ecologically optimal combination of a regenerative power supply (by the systems 300 and / or 400) and a conventional power supply, here represented by a part of a network 500, is preferably realized.
  • the entire system 100 therefore provides the regenerative electrical energy El largely directly
  • a corresponding converter 501 is used, as shown in FIG. 2 indicated in schematic form.
  • the corresponding system components or components are also referred to here as energy supply system 501.
  • an intelligent system controller 110 may, for. B. the
  • the plant controller 110 of FIG. 2 may be used in all embodiments with the plant controller 110 of FIG. 5 designed / realized as a common control. However, these controls 110 can also be designed / implemented separately in all embodiments. In principle, the respective currently available excess energy portion E2 is taken from the interconnected network 500, while the other
  • Solar power plant 300 and / or 400 (and / or from a wind power plant and / or from a hydroelectric power plant and / or from a wastewater treatment plant and / or from a biogas plant).
  • a wind power plant and / or from a hydroelectric power plant and / or from a wastewater treatment plant and / or from a biogas plant it is preferable for an intelligent reversal of the previous principle, in which the
  • Frequency control capacities for regenerative power plants in the Verbundnetz 500 vorzuhalten This principle allows the operator of a total plant 100 to include additional technical and economic parameters in the control of the overall plant 100. These parameters are so-called input quantities II, 12, etc., which are included in decisions by the controller 110. A part of the parameters can be specified within the controller 110 in a parameter memory 111. Another part of the parameters can come from the outside. Here, for example, price and / or availability information can be received from the operator of the interconnected network 500.
  • FIG. 3 a further overall system 700 is now shown schematically. A part of this total plant 700 corresponds to the entire plant 100 according to FIG. 2. In this respect, reference is therefore made to the preceding description of the corresponding elements.
  • Embodiment of FIG. 3 wholly or substantially (preferably more than 80%) from renewable energy sources 300 and / or 400 (or from other renewable energy sources).
  • Lines 112, 113 and 114 are shown. These lines 112, 113 and 114 control energy or mass flows of the entire system 100 or 700.
  • Processor of the controller 110 executes control software and makes decisions based on parameters programmed decisions.
  • Control / regulate energy and mass flows cause.
  • electrical signals sl, s2 control actuators Sl, S2, as shown in Figures 2, 3 and 5 indicated. This also applies to the other signals and actuators.
  • carbon dioxide 101 is used as a gaseous carbon source, as indicated schematically in Figures 2, 3 and 5.
  • the carbon dioxide 101 is derived from a combustion process or an oxidation process via C0 2 deposition (eg, a Silicon Fire
  • the carbon dioxide 101 can also be separated off from crude gas and provided or originate from one of the other sources mentioned above.
  • the carbon dioxide 101 can also come from other sources.
  • the carbon dioxide 101 is provided via a pipeline, a conduit, a steel bottle or a tank.
  • the DC power El is used in the illustrated embodiment to perform a water electrolysis to produce hydrogen 103 as an intermediate.
  • the electrolysis system respectively
  • FIG. 2 and FIG. 3 Performing such an electrolysis, is shown in FIG. 2 and FIG. 3 by the
  • the carbon dioxide 101 is with the
  • the corresponding (mixed) gas is referred to herein as the starting material AS.
  • reactor plant 50 of the invention is preferably in all
  • Embodiments of a part of the entire plant 100 or 700 Embodiments of a part of the entire plant 100 or 700.
  • a water electrolysis using DC El as mentioned.
  • the required hydrogen 103 is in an electrolysis plant 105 through the
  • the required (electrical) energy El for this reaction of 286.02 kJ / mol corresponds to 143010 kJ per kg of H 2 .
  • Reaction 2 gives the stoichiometry for the methanol synthesis. From a purely mathematical point of view, the starting material AS1 at the inlet 21 of the
  • Reactor 10 ideally a composition with 3 moles of H 2 per mole of C0 2 .
  • the composition should be approx. 3.05 to 3.10 moles of H 2 per mole of C0 2 , since it must have a slight excess of hydrogen 103.
  • all embodiments of the invention operate with about 3.05 to 3.10 moles of H 2 per mole of CO 2 .
  • the reactor 10 may include a fluid space 14 (see, eg, FIG.
  • the actual reaction area (s) inside the reactor 10 are surrounded by a reactor jacket and cooled by a fluid (preferably water).
  • a fluid preferably water.
  • Fig. 4 are a corresponding fluid supply 16 and a
  • Typical synthesis conditions in the synthesis reactor 10 are about 50 to 150 bar and about 250 ° C to 270 ° C.
  • the pressure is preferably between 50 and 100 bar.
  • the heat of reaction may, for. B. to other system elements, such as to an evaporator of a distillation column (which may be downstream of the process stage 200) or to other downstream plant areas "passed".
  • Reaction area / reaction areas of the reactor 10 carried out so that the reaction product liquid methanol 108 (or methanol-water mixture) is formed.
  • FIG. 2 and FIG. 3 is based on the dashed arrow 112
  • the controller 110 can regulate the energy flow El.
  • the arrow 112 represents a control or signal line.
  • Other possible control or signal lines 113, 114 are also shown.
  • the control or signal line 113 controls, for example, the C0 2 amount that is available for the reaction 106 in the reactor 10. If, for example, less hydrogen 103 is produced by the electrolysis 105, proportionally less C0 2 must be supplied.
  • the optional control or signal line 114 may regulate, for example, the amount of H 2 via an actuator Sl. Such a regulation makes sense if there is a hydrogen buffer, which can be taken from hydrogen 103, even if at the moment no hydrogen or less hydrogen by the electrolysis 105th (or by the use of elemental silicon) is produced.
  • an optional control or signal line 113 may control the C0 2 amount via an actuator S2.
  • an actuator S2 Preferably, in all embodiments of the invention, two actuators Sl, S2 followed by a static mixer 257 used to a process technically correct mixture of the components of the gaseous
  • Stoichiometrically correct mixing of the components 101 and 103 takes place, for example, using the controller 110 and a suitable measuring device 254 (preferably 3.05 mol to 3.10 mol of H 2 per mol of CO 2 as starting material AS
  • a reactor 10 or a reactor unit 50 is used, which at the outlet (at Domausiass 23) a methanol-containing material with a high methanol concentration (preferably a methanol-water mixture in the ratio 1: 1 (molar); 29.5 wt.% Water in crude methanol).
  • a methanol-containing material with a high methanol concentration preferably a methanol-water mixture in the ratio 1: 1 (molar); 29.5 wt.% Water in crude methanol.
  • an exemplary reactor 10 is shown in a schematic representation.
  • the reactor 10 has z. B. two input-side gas inlets 21, two output-side product outlets 23 a preferably a fluid space 14.
  • the fluid space 14 serves in a preferred mode of operation of the
  • a fluid e.g., water or gas
  • a fluid discharge 17 is provided on the fluid space 14 to remove the fluid.
  • a fluid e.g., water or gas
  • a fluid discharge 17 is provided on the fluid space 14 to remove the fluid.
  • a controller (which, for example, may be embodied as part of the (plant) controller 110) is provided
  • Reactor 10 is used which initially applies warm fluid to the fluid space 14 during the "start-up" of the reactor 10 to initiate the synthesis reaction, followed by the introduction of a cooled fluid to remove heat of reaction resulting from the exothermic synthesis Depending on the capacity of the reactor 10, reaction heat may be supplied by means of a fluid in the fluid space 14 and the synthesis reaction may proceed in the endothermic region.
  • the starting material AS and / or AS1 is preheated (eg by the
  • Heater / heat exchanger 267) and introduced into the reactor 10 at elevated pressure The pressure and the temperature depend on the type of catalyst.
  • the temperature can range between 100 and 350 degrees Celsius and the pressure between 15 and 150 bar.
  • the temperature is in the range between 200 and 280 degrees Celsius and the pressure between 50 and 100 bar.
  • the invention is used or used in a reactor system 50, which is shown in FIG. 5 is shown schematically.
  • the reactor plant 50 is designed specifically for the synthesis of a methanol-containing product 108.
  • the synthesis reaction 106 is carried out using a starting material AS1 which contains a gas having a carbon dioxide fraction 101 and a hydrogen fraction 103.
  • the reactor 10 of the reactor system 50 has a gas inlet 21 and a Product outlet 23, wherein at the product outlet 23 a process stage 200 is arranged.
  • This process stage 200 is designed to separate a product gas mixture PGG, which is provided at the product outlet 23, into a purge gas component PG, into a portion of the methanol-containing product 108 and into a recycle gas component KG.
  • the reactor system 50 further comprises a cycle gas recirculation 262 in order to recirculate the recycle gas component KG and to combine it with the starting material AS before the resulting mixed gas (here called AS1) can be fed to the gas inlet 21.
  • the reactor system 50 of the invention is characterized in that it comprises in all embodiments in addition to the recycle gas 262 a return line 250, the so with its line input 251 to the process stage 200 and with its line output 252 to the input stage 253 of the reactor system 50th is connectable, that at least a portion of the purge gas PG is attributable to the input stage 253 to be passed through the reactor 10 again.
  • the reactor system 50 includes a measuring device 254, which in the area of the input stage 253 for determining the current
  • Carbon (dioxide) proportion is arranged. It comes preferably one
  • Control device 255 is used, which may be part of the (plant) controller 110.
  • the control device 255 or the (plant) control 110 is designed to specify the carbon dioxide content and / or the hydrogen content and therefore controls / controls the input stage 253.
  • control device 255 or the (plant) controller 110 preferably controls the actuator S1 and / or the actuator S2.
  • the process control in the reactor system 50 is carried out using the control device 255 and / or the (plant) controller 110 so that the purge gas PG mainly only a carbon dioxide content and a
  • the purge gas portion PG may include a small amount of carbon monoxide. Due to process variations in the reactor system 50, the ratio between the carbon dioxide content, the hydrogen content and the carbon monoxide content at the outlet 23 of the reactor 10 is variable.
  • the controller 255 and / or the (plant) controller 110 are / are together with the measuring device 254 capable of this
  • the reactor 10 is, as described, filled with a catalyst for the catalytic conversion of the carbon dioxide content and the
  • Control device 255 and / or the (plant) controller 110 is a desired stoichiometry of the carbon dioxide content and the hydrogen content of the
  • Predetermined starting material AS1 which in all embodiments per mole
  • Carbon dioxide portion 101 preferably 3.05 to 3.10 moles of hydrogen has 103 shares. It should be noted here that depending on the catalyst, e.g. Also, a small excess of the hydrogen content 103 may be possible. In this case, the control device 255 and / or the (plant) controller 110 predefines a correspondingly adapted nominal stoichiometry. However, the kinetics of methanol synthesis 106 always requires a slight excess of hydrogen 103.
  • the conversion to the methanol-containing product 108 is incomplete because the reaction 106 is limited by a thermodynamic equilibrium.
  • the conversion of the reactants i.e., the proportion of carbon dioxide 101 and the proportion of hydrogen 103 in the starting material AS1
  • feedstocks (reactants) are discharged at the outlet of the reactor 10, but the proportionate amount thereof is always lower as the cycle ratio is increased.
  • the recirculating gas recirculation 262 preferably comprises in all embodiments a compressor 263 (also referred to as a recirculation gas compressor) which is used to reduce the proportion of circulating gas KG, which is recirculated through the recycle gas 262, from that of the recirculation gas
  • cycle gas ratio (P / E) 4 means that 4
  • the equilibrium and kinetics of the reaction 106 for the product 108 are favorably influenced by the dilution of the reactants in the reaction gas.
  • a product gas mixture PGG is output.
  • the synthesis reaction 106 requires a minor one
  • purge gas PG comprises in the present process management essentially carbon dioxide, hydrogen and a low carbon monoxide content, the ratio between the
  • Carbon dioxide, the hydrogen and the carbon monoxide component is variable. This variability results from a whole series of parameters, such as pressure fluctuations, saturation of the catalyst 60, degree of consumption of the catalyst, temperature fluctuations, etc. in the reactor system 50.
  • the amount of purge gas per se is not a (strongly) variable variable.
  • the input stage 253 of FIG Reactor 50 have a fresh gas supply 264 for hydrogen gas 103 and carbon dioxide gas 101.
  • Fresh gas supply 264 each have an actuator Sl or S2 to the
  • Actuators S1 and S2 are preferably controlled in all embodiments by the control device 255 and / or by the (plant) controller 110.
  • FIG. 5 embodiment shown includes
  • Reactor 50 a flow control 265 to determine the flow rate can.
  • the two fresh gases 103 and 101 are fed via a supply line 258 in the static mixer 257, so as to obtain a homogenized mixture of the fresh gases 103 and 101.
  • the static mixer 257 preferably, the
  • both the return line 250 and the supply line 258 are in FIG.
  • the purge gas PG is preferably in Low pressure range fed in front of the fresh gas compressor 260.
  • the controller 255 is disposed between the static mixer 257 and the fresh gas compressor 260 to flow directly in the flow of the
  • the electrical signal sl of the measuring device 254 drives preferably at all
  • the actuator Sl (the mass flow controller) of the actuator
  • the signal value of the starting material AS without the purge gas recirculation 250 serves as a setpoint.
  • Flow control 265 (eg in the form of a flow controller), which is arranged downstream of the measuring device 254 in the flow direction SR.
  • Flow control 265 preferably drives actuator S2 (the mass flow controller) of the carbon dioxide flow in all embodiments.
  • Feed gas mixture EGG brings from the low pressure area into the high pressure area.
  • the output line 261 of the fresh gas compressor 260 is merged with a line 266 of the recycle gas 262.
  • the cycle gas recirculation 262 comprises a cycle gas compressor 263.
  • a heater / heat exchanger 267 follows on the input side of the reactor 10. This heater / heat exchanger 267 heats the starting material AS1, as required.
  • an actuator S3 and a flow control 268 may be provided in the area downstream of the recycle gas compressor 263.
  • the flow control 268 controls the actuator S3 by means of an electrical signal s3.
  • the downstream process stage 200 preferably comprises the following elements in all embodiments.
  • the (gas) outlet 23 feeds a final cooler 269. Behind this final cooler 269 are a
  • each of the separators 270, 271 may be an associated
  • Actuator S4, S5 follow as shown.
  • Each of the actuators S4, S5 is controlled by a level indicator 272, 273 (LIC, Level indicator controller). That the level gauge 272, 273 together with the respective actuator S4, S5, a level control.
  • the corresponding electrical signals are referred to here as s4, s5.
  • Low pressure separator 271 delivered.
  • the methanol content (residual methanol) of the cycle gas KG is only determined by the pressure and temperature of the final cooler 269.
  • the corresponding circulating gas stream is as follows: outlet 23 final cooler 269 high-pressure separator 270 outlet 274 circulating gas compressor 263 line 266 heater / heat exchanger 267 inlet 21 reactor
  • Raw methanol is withdrawn as follows: outlet 23 final cooler 269 high-pressure separator 270 outlet 275 low-pressure separator 271 outlet 276 outlet 201. After the outlet 201, a line, a tank or a distillation stage can follow.
  • the purge gas PG can be removed via an output 277, as already described.
  • the pressure of the Niederbuchabscheiders 271 at the output 278 should be set slightly higher are considered to be the pressure of the fresh gas AS in front of the static mixer 257 in order to be able to incorporate the gas flow of the release gas LG into the purge gas return line 250.
  • the purge gas PG and possibly also the release gas LG is fed via the return line 250 back to the input stage 253.
  • only purge gas PG is fed back to the input stage 253 and the release gas LG is delivered via a line 279.
  • purge gas PG can be controlled in all embodiments via a pressure display controller 280 and a corresponding actuator S6, which is controlled with an electrical signal s6.
  • a flow control 282 may be arranged with a further actuator S7 to deliver purge gas PG, if necessary, instead of leading back according to the invention.
  • a pressure display controller 283 and a corresponding actuator S8, which is controlled by an electrical signal s8, can be used (see FIG. 5).
  • an optional connection line 284 is arranged according to the invention, the dissolving gas LG e.g. can be taken at a point after the actuator S8 and introduced into the area where the line input 251 of the return line 250 attaches.
  • the optional connection line 284 is indicated by a dotted arrow. This release gas recirculation is optional.
  • Feed gas mixture EGG and the cycle gas KG also take place before the compressor 263.
  • the compressor 263 In the in Fig. 6 approach, the compressor 263 must be dimensioned slightly larger than in Fig. 5.
  • the in FIG. 6 variant can be used in all embodiments of the invention.
  • the carbon dioxide content in all embodiments in the supply line 256 is determined / measured.
  • Conductivity sensor (as part of a measuring device 254 on the supply line 256) provides a reliable and reproducible indication that it is the
  • Control device 255 and / or the (plant) control 110 makes it possible to intervene in order to increase or decrease the proportion of the freshly supplied carbon dioxide gas 101 and / or the hydrogen gas 103 so that the predetermined desired stoichiometry of the feed gas composition AS1 can essentially be maintained , Furthermore, it has been found that the feed gases 101, 103 are very pure are and therefore have no or very low levels of unreactable interfering or even harmful components. Therefore, even in the purge gas PG despite concentration only very small amounts of these
  • the composition of the purge gas stream PG is very different from the desired feed gas composition AS1, it is necessary to reduce the amount of fresh feed gases, ie. the carbon dioxide gas 101 and / or the hydrogen gas 103, adjust accordingly.
  • the invention makes its way over the already mentioned thermal conductivity measurement using at least one conductivity sensor 259.
  • the very different thermal conductivity of the gases H 2 and C0 2 is measured using a thermal conductivity detector (analyzer). Sensor 259) determines the gas stream to be analyzed with sufficient accuracy. The chromatographic splitting of the gas can be dispensed with.
  • FIG. 5 is a preferred embodiment , which uses a measuring device 254 to conduct an analysis of the instantaneous gas flow in the supply line 256
  • the measuring device 254 is preferably at all
  • the electrical signal sl of the measuring device 254 drives the mass flow controller S1 of the hydrogen flow.
  • the setpoint is the signal size of the fresh gas H 2 without
  • the volume control of the total fresh gas flow (H 2 and C0 2 ) is preferably carried out in all embodiments by the flow controller 265, arranged in the gas flow to the measuring device 254. Its signal s2 drives, for example, the mass flow controller S2 of the C0 2 stream.
  • Purge gas loss actually has a small effect on the fresh gas requirement, if the purge gas PG as previously, for example, simply released into the environment. For example, in a reference system 50, approximately 1% of C0 2 and 3% of H 2 would be lost under design conditions in Purgegas PG. But the high prices of the pure feed gases 101, 103 and the complete avoidance of the exhaust gas losses and the exhaust emissions make the small additional
  • An advantage of the invention is the avoidance of exhaust emissions.
  • C0 2 utilization has heretofore been more than 98% designed to "lose" only about 2% of C0 2 in the process.
  • reactor 50 can be designed to operate at substantially lower conversions This makes it possible to reduce the reactor volume of the reactor 10 and the associated circuit 262. This is particularly noticeable in the case of investment costs for the reactor 10, which must preferably be designed for high pressures in the range between 50 and 100 bar.
  • the reactor 10 is particularly suitable for the synthesis of regenerative methanol CH 3 OH from carbon dioxide C0 2 and hydrogen H 2 , if the hydrogen H 2 via the (endothermic) electrolysis of water with
  • Embodiments of course can also be used for other synthesis processes and that the synthesis can be operated with regenerative energy and / or with regenerative starting material AS, but also with fossil energy and / or with fossil starting material AS.
  • the synthesis gas from carbon dioxide and hydrogen or from a very small amount of carbon monoxide, and larger proportions of carbon dioxide 101 and hydrogen 103 can be implemented in a reactor 10 according to the invention using a suitable catalyst for each of methanol 108 and a methanol-containing product 108, such as described.
  • a suitable catalyst for each of methanol 108 and a methanol-containing product 108 such as described.
  • copper-based catalysts eg., CuO catalysts
  • zinc oxide catalysts eg ZnO catalysts
  • Chromium oxide-zinc oxide catalysts are used. All other known catalysts are suitable for use in a reactor 10.
  • the catalyst may also comprise a suitable carrier (eg carbon, silicate, aluminum (eg Al 2 O 3 ) or ceramic).
  • a suitable carrier eg carbon, silicate, aluminum (eg Al 2 O 3 ) or ceramic.
  • Metallic catalysts can also be used an organic catalyst.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un système de réacteur (50) servant à synthétiser un produit (108) contenant du méthanol en utilisant une charge de départ (AS1) qui contient un gaz comprenant une fraction carbone (101) et une fraction hydrogène (103). Le réacteur (10) possède une arrivée de gaz (21) et une sortie de produit (23) au niveau de laquelle est disposé un étage de traitement (200) adapté pour séparer un mélange de produits gazeux (PGG) en une fraction du produit (108) contenant du méthanol et en une fraction de gaz circulant (KG), ledit étage donnant également une fraction de gaz de purge (PG). Le système de réacteur (50) comprend en outre un recyclage de gaz circulant (262) qui permet de renvoyer la fraction de gaz circulant (KG) en direction de l'arrivée de gaz (21). Le système comporte une conduite de recyclage (250) qui est reliée à l'étage de traitement (200) et à un étage d'entrée (253) de façon à pouvoir recycler une partie au moins de la fraction de gaz de purge (PG) vers l'étage d'entrée (253) en vue de la renvoyer dans le réacteur (10). Le système utilise un dispositif de mesure (254), adapté pour déterminer la fraction carbone instantanée, ainsi qu'un dispositif de commande (110, 255) servant à prédéfinir le rapport de la fraction carbone sur la fraction hydrogène.
EP13721306.2A 2013-04-26 2013-04-26 Procédé et système de réacteur de synthèse de méthanol avec recyclage du gaz circulant et du gaz de purge Withdrawn EP3016924A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2013/058682 WO2014173452A1 (fr) 2013-04-26 2013-04-26 Procédé et système de réacteur de synthèse de méthanol avec recyclage du gaz circulant et du gaz de purge

Publications (1)

Publication Number Publication Date
EP3016924A1 true EP3016924A1 (fr) 2016-05-11

Family

ID=48326275

Family Applications (1)

Application Number Title Priority Date Filing Date
EP13721306.2A Withdrawn EP3016924A1 (fr) 2013-04-26 2013-04-26 Procédé et système de réacteur de synthèse de méthanol avec recyclage du gaz circulant et du gaz de purge

Country Status (2)

Country Link
EP (1) EP3016924A1 (fr)
WO (1) WO2014173452A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102016213668A1 (de) 2016-07-26 2018-02-01 Thyssenkrupp Ag Verfahren und Anlage zur Herstellung von Alkoholen oder Kohlenwasserstoffen
DK3491173T3 (da) * 2016-07-26 2022-07-11 Thyssenkrupp Ind Solutions Ag Fremgangsmåde og anlæg til fremstilling af methanol
DE102019113003A1 (de) 2019-05-16 2020-11-19 Thyssenkrupp Ag Verfahren und Anlage zur Synthese von Methanol

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5147937A (en) 1990-03-22 1992-09-15 Rohm And Haas Company Process for making controlled, uniform-sized particles in the 1 to 50 micrometer range
DE19605572A1 (de) 1996-02-15 1997-08-21 Metallgesellschaft Ag Verfahren zum Erzeugen von Methanol
DE19644216A1 (de) * 1996-10-24 1998-04-30 Metallgesellschaft Ag Verfahren zum Erzeugen von Methanol aus Erdgas
US6642280B2 (en) * 2001-08-09 2003-11-04 Air Products And Chemicals, Inc. Control scheme for conversion of variable composition synthesis gas to liquid fuels in a slurry bubble column reactor
US20100175320A1 (en) * 2006-12-29 2010-07-15 Pacific Renewable Fuels Llc Energy efficient system and process for the continuous production of fuels and energy from syngas
DE102008049622B4 (de) 2008-09-30 2012-10-31 Lurgi Gmbh Verfahren und Anlage zur Herstellung von Methanol
WO2010069385A1 (fr) 2008-12-18 2010-06-24 Silicon Fire Ag Procédé de préparation d'un vecteur d'énergie
EP2647596A3 (fr) 2008-12-18 2014-08-27 Silicon Fire AG Procédé et appareil pour fournir une source d'énergie en utilisant du dioxyde de carbone comme source de carbone et de l'énergie électrique
EP2226290A3 (fr) 2009-03-04 2013-12-04 Silicon Fire AG Procédé de préparation et d'utilisation d'un support d'énergie, notamment pour véhicules
EP2228358A1 (fr) * 2009-03-13 2010-09-15 Methanol Casale S.A. Récupération de CO2 dans un processus de synthèse de méthanol
DE102011017300A1 (de) * 2011-04-15 2012-10-18 Lurgi Gmbh Verfahren und Anlage zur Herstellung vom Methanol aus inertenreichem Synthesegas
US8168685B2 (en) * 2011-07-01 2012-05-01 Membrane Technology And Research, Inc Process for the production of methanol including one or more membrane separation steps

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
None *
See also references of WO2014173452A1 *

Also Published As

Publication number Publication date
WO2014173452A1 (fr) 2014-10-30

Similar Documents

Publication Publication Date Title
EP2464617B1 (fr) Procédé et installation de production d'une ressource énergétique à base d'hydrocarbure en utilisant une fraction de méthanol produit par régénération et une fraction de méthanol qui est produit par oxydation directe ou par oxydation partielle ou par reformage
EP2491998B1 (fr) Procédé de recyclage de de produits de combustion de combustibles fossiles
EP2516358B1 (fr) Procédé de production d'un gaz de produit riche en méthane, et système de réacteur utilisable à cet effet
EP3491173B1 (fr) Procédé et dispositif de fabrication du méthanol
DE10392525B4 (de) Verfahren, Prozesse, Systeme und Vorrichtung mit Wasserverbrennungstechnologie zur Verbrennung von Wasserstoff und Sauerstoff
DE202009019105U1 (de) Anlage zum Bereitstellen eines Energieträgers unter Einsatz von Kohlenstoffdioxid als Kohlenstofflieferant und von elektrischer Energie
DE102012216090A1 (de) Grüne Verbundanlage zur Herstellung von chemischen und petrochemischen Produkten
EP2438982A1 (fr) Procédé de préparation et d'utilisation d'un alcool et utilisation de l'alcool pour l'augmentation du degré d'action et de la puissance d'un moteur à combustion interne
EP2562237B1 (fr) Procédé de préparation d'un gaz à très forte teneur en méthane et installation conçue dans ce but
EP2624947B1 (fr) Procédé et installation de synthèse d'hydrocarbure
EP3642394A1 (fr) Dispositif de transformation d'énergie pour la transformation d'énergie électrique en énergie chimique, réseau comprenant un tel dispositif de transformation d'énergie et procédé permettant de faire fonctionner un tel dispositif de transformation d'énergie
EP2935558A2 (fr) Système de conversion d'énergie
EP3016924A1 (fr) Procédé et système de réacteur de synthèse de méthanol avec recyclage du gaz circulant et du gaz de purge
DE102012105736A1 (de) Verfahren zur Speicherung von Elektroenergie
EP2682450B1 (fr) Procédé de méthanisation catalytique et installation de méthanisation
EP2650257B1 (fr) Dispositif de synthèse de méthanol régénératif à partir de gaz méthane contenant du co2
EP1887071A1 (fr) Procédé de production d'hydrocarbures synthétiques et leurs dérivés à partir de dioxide de carbone et de dihydrogène utilisés comme gaz de synthèse
DE112008001851T5 (de) Erzeugung von Naturgas unter Verwendung eines gasdynamischen Lasers mit Stromerzeugung durch Kraft-Wärme-Kopplung
EP2438980A1 (fr) Procédé et dispositif de préparation et d'installation de méthanol à base d'hydrogène à des fins de dénitrification
EP2760989B1 (fr) Installation de biogaz et procédé pour faire fonctionner une installation de biogaz
DE102018106076A1 (de) Verfahren und Anordnung zur Methanolsynthese
WO2014060168A2 (fr) Dispositif de compression de gaz naturel et procédé de production de méthane
DE102021122602B4 (de) Anlage und Verfahren zur kontinuierlichen Herstellung von Ammoniak unter Verwendung von erneuerbaren Energien
DE102018213482A1 (de) Bereitstellung von Kohlenstoffdioxid mittels sauerstoffbasierter Verbrennung
EP4396127A1 (fr) Installation et procédé pour la production continue d'ammoniac à l'aide d'énergies renouvelables

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20160307

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAX Request for extension of the european patent (deleted)
RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: SILICON FIRE AG

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20171027

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20211103