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WO2019149435A1 - Réacteur tubulaire et son procédé de fonctionnement - Google Patents

Réacteur tubulaire et son procédé de fonctionnement Download PDF

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Publication number
WO2019149435A1
WO2019149435A1 PCT/EP2018/097025 EP2018097025W WO2019149435A1 WO 2019149435 A1 WO2019149435 A1 WO 2019149435A1 EP 2018097025 W EP2018097025 W EP 2018097025W WO 2019149435 A1 WO2019149435 A1 WO 2019149435A1
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WO
WIPO (PCT)
Prior art keywords
reaction zone
density
temperature
tubular reactor
hydrogen
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.)
Ceased
Application number
PCT/EP2018/097025
Other languages
German (de)
English (en)
Inventor
Thomas Stiegler
Jakob Albert
Manfred Baldauf
Katharina Meltzer
Alexander Tremel
Peter Wasserscheid
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 WO2019149435A1 publication Critical patent/WO2019149435A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • B01J8/02—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
    • B01J8/04—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 passing successively through two or more beds
    • B01J8/0446—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 passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449—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 passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—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 passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • 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
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • 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
    • B01J8/04—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 passing successively through two or more beds
    • B01J8/0403—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 passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
    • B01J8/0407—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 passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
    • B01J8/0415—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 passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being superimposed one above the other
    • 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
    • B01J8/04—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 passing successively through two or more beds
    • B01J8/0403—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 passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
    • B01J8/0423—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 passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds
    • B01J8/0426—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 passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds the beds being superimposed one above the other
    • 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
    • B01J8/04—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 passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • 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

Definitions

  • the invention relates to a tubular reactor for converting hydrogen to methane and a method for operating the tubular reactor.
  • Electricity generation fluctuates with increasing share of electricity from renewable energies during the course of the day.
  • controllable power plants or storage facilities are needed to store this energy.
  • One of the currently contemplated solutions is the conversion of electrical energy into value products, in particular organic platform chemicals or synthesis gas comprising carbon monoxide and hydrogen.
  • One possible technique for converting electrical energy into value products is electrolysis.
  • the electrolysis of water to hydrogen and oxygen is a method known in the art.
  • the hydrogen produced in the electrolysis process can react with a component comprising carbon dioxide to form methane and water.
  • the methane can then advantageously be fed directly into the existing natural gas infrastructure.
  • the object is achieved with a tubular reactor according to claim 1 and a method for operating a tubular reactor according to claim 14.
  • the tubular reactor according to the invention for converting hydrogen to methane comprises a first reaction zone with a first catalyst bed having a first density and a temperature in a first temperature range. Furthermore, the tubular reactor comprises a second reaction zone with a second Kata lysatorbett having a second density and a temperature in a second temperature range. Furthermore, the tubular reactor comprises a third reaction zone with a third cata- torbate having a third density and a temperature in a third temperature range, the first density being lower than the first density. half of the second density, and the second density is below the third density. In other words, the density of the catalyst bed increases in the direction of flow of the educt gas, in particular of the hydrogen.
  • the reaction zones are arranged in the tubular reactor in the flow direction one behind the other.
  • the inventive method for operating the tubular reactor for converting hydrogen to methane comprises several
  • a tubular reactor having at least three reaction zones wherein each of the three reaction zones comprises a catalyst bed.
  • each reaction zone comprises a catalyst bed having a defined density, where the respective densities of the catalyst bed increase in the flow direction of the educt gas.
  • a reactant gas comprising hydrogen and carbon dioxide is added to a first reaction zone.
  • this first reaction zone is a temperature in a first temperature range, in which a first portion of hydrogen and carbon dioxide is converted to a first portion of methane.
  • both the unreacted educt gas, in particular the hydrogen and the carbon dioxide, and the methane are fed into a second reaction zone.
  • a second portion of methane is produced at a temperature in a second temperature range from a second hydrogen fraction and the carbon dioxide.
  • This second methane content is greater than the first methane content.
  • a larger amount of methane is produced in the second reaction zone than in the first reaction zone.
  • the educt gas, which comprises unreacted hydrogen, and the methane, which was prepared in the first and second reaction zone are fed into a third reaction zone.
  • a third portion of the hydrogen is reacted with carbon dioxide to form a third portion of methane at a temperature in a third temperature range.
  • the guiding of the educt gas comprehensively allows hydrogen through the different reaction zones increasing catalyst bed density, a flexible reaction of hydrogen and carbon dioxide without the use of a large cost-intensive hydrogen storage and without the use of a temperature control during a reaction interruption, so that the flexible reaction of hydrogen is possible with low energy consumption.
  • the first reaction zone represents a start-up zone.
  • the first temperature range of this zone should expediently be above a minimum temperature which is above the reaction ignition temperature and above the condensation temperature of water, in particular 100 ° C.
  • the first reaction zone comprises the catalyst bed with the lowest density.
  • the second reaction zone has a temperature in a second temperature range. In particular, this should be below the temperature that limits the stability of the cata- sector. In this zone, the largest conversion of hydrogen takes place.
  • the second catalyst bed has a higher density compared to the first reaction zone.
  • the hydrogen is reacted, which was not yet reacted in the first two reaction zone. It is advantageous if the temperature in the third temperature range is lower than in the second temperature range Tempe. As in the first reaction zone, the temperature in this third reaction zone should, however, advantageously be above the condensation temperature of water and above the reaction start temperature. This is achieved by a particularly dense catalyst bed.
  • the third reaction zone has a catalyst bed with a third density, this third density being higher than the first and second densities, ie having the highest density of the tubular reactor. Since the educt gas volume flow can fluctuate at the beginning of the respective zone and a conversion in the respective reaction zone is still guaranteed, this reactor structure can be operated with fluctuating educt gas stream.
  • the entire volume flow fluctuates of the educt gas.
  • the ratio of hydrogen and carbon dioxide remains constant in the educt gas, in particular a stoichiometric ratio of the educt gases is set.
  • the third reaction zone ensures that a residual amount of hydrogen is reacted, which may be low or high depending on the input volume flow of educt gas.
  • reaction zones dersel ben type ie in particular te with the same Katalysatorbettdich. These are then separated from each other by a feeding device for the cooling medium.
  • a supply device for a cooling fluid is arranged between the second and third reaction zone.
  • a cooling fluid is added directly into the third reaction zone.
  • the third reaction zone is cooled by means of an indirect cooling, in particular via an introduced heat exchanger.
  • direct cooling by means of a cooling fluid in particular water
  • a cooling fluid in particular water
  • the conversion of hydrogen to methane is exothermic, thereby releasing at a high conversion a high amount of energy that must be brought out of the system before the mixture of hydrogen and methane flows through the third reaction zone.
  • the temperature in the third Temperaturbe is rich below the temperature in the second Temperaturbe rich. Since the density of the catalyst bed in the third reaction zone but above the second density of the cata- torbett in the second reaction zone, it is ensured tet the fact that the proportion of hydrogen, which was not reacted in the first two reaction zone, is reacted here.
  • Advantageously contributes to both the high catalyst bed density, as well as the low temperature in the third reac tion zone, since it is an exothermic reaction.
  • the temperature in the first reaction onszone in a first temperature range ranging from 100 ° C to 400 ° C. Particularly advantageous is the temperature in the first temperature range between 150 ° C and 250 ° C.
  • the heat generated in the first reaction zone is transported into the second reaction zone by means of the educts and products and thus used to heat the second reaction zone.
  • the inlet temperature in the first reaction zone, in the second reaction zone and / or in the third reaction zone is adjusted depending on the volume flow of the educt gas.
  • the heating power in the first zone is turned down, since the residence time of the educt gas in the first reac tion zone is higher and thus proportionately more reactant gas can be set.
  • the inlet temperature, in particular in the first reaction zone is set higher because the residence time of the educt gas in the first reaction zone is shorter.
  • the proportionate, in other words relative to the Eduktgasmenge, sales is lower than at low Eduktgasströmen.
  • the maximum temperature of the second temperature range is 500 ° C.
  • this maximum temperature is chosen such that both the strength of the reactor material and the Sta can be ensured stability of the catalyst.
  • a high conversion of hydrogen is achieved with carbon dioxide to methane, resulting in high amounts of heat. This heat must be dissipated so as not to exceed the maximum temperature.
  • This can be done by means of indirect cooling, in particular by the introduction of cooling media through flow components, in particular in the form of heat exchangers.
  • a direct cooling by means of a cooling fluid, in particular water can be carried out, the water being injected into the second reaction zone.
  • the temperature in the third temperature range is between 200 ° C and 400 ° C. Particularly advantageous is the temperature in the third temperature range between 250 ° C and 350 ° C.
  • the temperature in the third temperature range is below the temperature of the second temperature range at high catalyst bed density, thereby ensuring that the unreacted hydrogen material and the carbon dioxide in the third reaction zone is converted to methane.
  • the first reaction zone comprises a Hei tion.
  • This heater advantageously ensures that the mini maltemperatur is reached for the reaction start. Furthermore, the heater ensures that the temperature is above the condensation temperature of the water. Water is produced as a product during the conversion of the hydrogen with carbon dioxide to methane. Additional water can be fed into the tubular reactor as cooling fluid as needed. The water should be in vapor form to maintain the stability of the catalyst bed.
  • the first, the second and / or the third catalyst bed comprise a porous metal structure for accommodating the catalyst.
  • the metal structure is advantageously electrically conductive.
  • such metallic Grundstruktu ren a high thermal conductivity and high electrical conductivity.
  • these structures allow a high surface area to volume ratio, allowing for efficient heat input into the reactor.
  • the heat input can via a heating of the reactor wall, which is in direct contact with the metal structure, take place. This allows a better heat input compared to conventional catalyst pellets. This is particularly advantageous in the first reaction zone.
  • the metal structure may be connected to electrodes. By applying a voltage to the electrodes and the electrical resistance in the metal structure, a temperature increase of the metal structure, it can be sufficient.
  • the contacting of the metal structure with Elekt roden allows even faster heat input in the United equal to the contacting of the metal structure with a Hei tion.
  • the rapid heating of the first reaction zone is particularly advantageous if the reactor is cooled at an interruption of the Eduktzussel below a minimum temperature and therefore must be heated quickly when re-use of the reactor to reach the starting temperature to it.
  • the catalyst is introduced as a porous bulk material in the tubular reactor.
  • An alternative embodiment and development of the inven tion is to coat a metal structure with catalyst.
  • Particularly advantageous is the combination of a metal-coated catalyst structure, which is coated with electrodes. is bound to achieve a direct and therefore advantageous fast heating of the metal structure and thus of the cata- gate.
  • the hydrogen comes from the electrolysis of water.
  • the tubular reactor with the three reaction zones with the fluctuating hydrogen flow from the electrolysis in dependence on the available electrical energy can be operated dynamically.
  • FIG. 2 shows a tube reactor with three reaction zones, reaction onsumsatz and three temperature ranges.
  • FIG. 3 shows a metal structure of a catalyst bed of the
  • FIG. 4 shows a process diagram of the methanation of the hydrogen by means of the tubular reactor.
  • FIG. 1 shows a tube reactor 1 having a first reaction zone 11, a second reaction zone 12 and a third reaction zone 13.
  • the first reaction zone 11 comprises a first catalyst bed 14 having a first density.
  • the second reaction zone 12 comprises a second catalyst bed 15 having a second density.
  • the third reaction zone 13 comprises a third catalyst bed 16 having a third density.
  • the reaction zones are in the tubular reactor 1 in a row Lich respect of the flow direction of the educt gas including hydrogen material 2 and carbon dioxide 3 is arranged. Between the second reaction zone 12 and the third reaction zone 13 there is a supply device 9 for a cooling fluid. At the end of the tubular reactor 1, methane 4 and water 5 leave the tubular reactor 1 as product stream.
  • the density of the catalyst bed in the respective reaction zone increases in the direction of the flow of educt gas. That is, the first reaction zone has the catalyst bed with the lowest density, the third reaction zone, the catalyst bed with the highest density.
  • the catalyst is particularly advantageously arranged in a metal structure 30. This metal structure is explained in more detail in FIG.
  • FIG. 2 also shows the tubular reactor 1 with the first reaction zone 11, the second reaction zone 12 and the third reaction zone 13. Furthermore, FIG. 2 shows a y-axis 8 in the longitudinal direction of the tubular reactor 1, ie in the flow direction of the educt gas Length of the tubular reactor 1 describes. FIG. 2 shows, transversely to the flow direction of the educt gases, an x-axis 7 which describes both the reaction conversion and the temperature ranges.
  • the methanation reaction can be described by Equation 1.
  • first reaction zone 11 with the first catalyst bed 14 with a first density ei ne start-up zone for the methanation reaction of Equation 1 represents.
  • a first temperature prevails in a first temperature range between 100 ° C and 400 ° C, more preferably between 150 ° C and 250 ° C.
  • This temperature range is set in Figure 2 as a tape is.
  • the temperature must suitably exceed the reaction onset temperature.
  • the temperature should be above 100 ° C, so that during the reaction tion resulting vapor water.
  • FIG. 2 shows on the basis of the conversion that the reaction starts in this first reaction zone.
  • the density of the catalyst bed 14 in this first reaction zone 11 is low in order to avoid pronounced temperature peaks due to the exothermic reaction. On the other hand, the density of the catalyst bed 14 must be sufficiently high to produce so much heat that the heating of the following second reaction zone 12 can be ensured. The amount of heat generated in the first reaction zone 11 is used to heat the second reaction zone 12 by convection.
  • FIG. 2 further shows that the second reaction zone 12 has a higher temperature level than the first reaction zone 11.
  • the temperature in the second reaction zone 12 is typically at most 600 ° C, especially at most 500 ° C. This maximum temperature must not be exceeded in order to maintain the strength of the reactor material and the stability of the catalyst.
  • FIG. 2 also shows that the greatest reaction conversion takes place in this second reaction zone 12. Due to the higher catalyst torêt this high turnover is possible. However, the conversion in this second reaction zone 12 is limited by the temperature, since the maximum temperature must not be exceeded despite the exothermic reaction.
  • FIG. 2 further shows that the temperature in the third reaction zone 13 is below the temperature in the second reaction zone 12.
  • the temperature in the third reaction zone 13 is typically in a range of 200 ° C to 400 ° C, more preferably in a range of 250 ° C to 350 ° C. In order to achieve these temperature differences from the second reaction zone 12 into the third reaction zone 13, it may be necessary for cooling to take place either between the two reaction zones or within the third reaction zone 13.
  • 9 is added by means of Zuzhouvorrich device as coolant water 5. It is about in this example, therefore, a direct cooling.
  • the third reaction zone 13 is ge indirectly cooled by means of heat exchanger structures. Water as a coolant is particularly advantageous in the direct cooling, since it on the one hand, in particular due to the enthalpy of vaporization, can achieve a sufficiently large cooling effect and on the other hand already as Pro product in the tubular reactor 1 is present, so that no addi tional components must be performed in the system.
  • the third catalyst density 16 should be higher than the first two catalyst bed densities in order to achieve a sufficient reaction rate at low temperatures and low educt concentrations. As in the first reaction zone 11, the temperature range is limited downwards by the reaction start temperature and the condensation temperature of the water 5.
  • Figure 2 illustrates that after the third reaction zone 13 almost full conversion is achieved.
  • the three reaction zones 11, 12, 13 allow by the un ferent densities of the three catalyst beds 14, 15 and
  • the cooling fluid water 5 can be guided flexibly in different amounts through the supply device 9 and so the third reaction zone accordingly the conversion and the temperature of the first two reac tion zones temperature such that the educt gas hydrogen 2 with carbon dioxide 3 almost completely to methane vice versa.
  • a large hydrogen storage for storing the hydrogen in times of high hydrogen production is advantageously not necessary.
  • FIG. 1 and FIG. 2 show by way of example that the second reaction zone has the greatest length. In this second reaction zone, the highest conversion is achieved. Both in Figure 1 and in Figure 2, three reaction zones are provided. But it is especially possible that several second reaction zones 12 are arranged one behind the other. Then, the length of the second reaction zone 12 may be smaller. In this case, it is expedient that water supply means for the coolant are present between these second reaction zones 12 in order to achieve a temperature below the maximum temperature for each of the second reaction zones 12.
  • FIG. 3 shows a metal structure 30 on which the cata- capacitor can be applied.
  • This metal structure 30 has in particular a diamond unit cell, which has spaces between.
  • the Me tall Vietnamese was coated with catalyst, so that a cata- sator für 32 is formed on the metal substrate 33.
  • this metallic basic structure has a high heat conductivity and a high electrical conductivity.
  • this structure has a high surface to Volumenver ratio, which allows effective heat input into the reactor 1.
  • the heat input into the tubular reactor 1 can take place via the heating of a reactor wall of the tubular reactor 1. Then it is useful if the reactor wall of the tube reactor 1, the tall tall structure 30 Me directly contacted.
  • the metal structure 30 is contacted by electrodes and heated when a voltage is applied due to the electrical resistance. This allows a very efficient and rapid heating of the metal structure 30, which makes the heat input into the Rohrreak gate 1 energy-efficient.
  • the cooled Rohrre actuator 1 can be heated electrically quickly and thus quickly return the operating temperature of the first reaction zone 11 he testifies.
  • This coated metal structure 30 is particularly advantageous in the first reaction zone 11 before. But it is also possible that the metal structure 30 in the second reaction zone 12 and in the third reaction zone 13 is arranged.
  • FIG. 4 schematically shows the interconnection of the tubular reactor 1, ie the methanation 10, with the electrolysis 40, a treatment plant 50 and the natural gas network 60.
  • Water 5 is split into hydrogen 2 and oxygen 17 by means of electrical energy, in particular if excess energy is present in a large amount of wind and sun.
  • the hydrogen 2 is fed into the tubular reactor 1 to methanation 10.
  • carbon dioxide 3 is supplied.
  • metha nization 10 is made of the carbon dioxide 3 and the water methane 4 and water 5 produced.
  • the methane 4 is then fed into a methane treatment plant 50, where it is worked up so that it can be Gelei tet in the natural gas network 60.
  • the methane 4 is used for subsequent reactions.
  • Another alternative is the onset of methane as a fuel, especially for locomotion means, especially vehicles.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un réacteur tubulaire et un procédé pour faire fonctionner ce réacteur tubulaire servant à convertir de l'hydrogène en méthane. Le réacteur tubulaire comprend trois zones de réaction. La première zone de réaction comprend un premier lit catalytique présentant une première densité et une température située dans une première plage de températures, la deuxième zone de réaction comprend un deuxième lit catalytique présentant une deuxième densité et une température située dans une deuxième plage de températures, la troisième zone de réaction comprend un troisième lit catalytique présentant une troisième densité et une température située dans une troisième plage de températures, la première densité étant inférieure à la deuxième densité et la deuxième densité étant inférieure à la troisième densité. Cela signifie que les densités du lit catalytique augmentent en direction du flux de gaz de départ. Ceci permet avantageusement un fonctionnement dynamique du réacteur tubulaire pour la méthanisation.
PCT/EP2018/097025 2018-02-01 2018-12-27 Réacteur tubulaire et son procédé de fonctionnement Ceased WO2019149435A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102018201561.9 2018-02-01
DE102018201561.9A DE102018201561A1 (de) 2018-02-01 2018-02-01 Rohrreaktor und Verfahren zum Betreiben eines Rohrreaktors

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CN115304440A (zh) * 2022-08-25 2022-11-08 北京航天试验技术研究所 一种火星表面运载火箭推进剂原位制备一体化系统及方法
CN115364807A (zh) * 2022-08-25 2022-11-22 北京航天试验技术研究所 一种用于火星表面二氧化碳加氢甲烷化的Sabatier反应器及方法

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