CN115364807A - Sabatier reactor and method for carbon dioxide hydromethanation on Mars surface - Google Patents
Sabatier reactor and method for carbon dioxide hydromethanation on Mars surface Download PDFInfo
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 26
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 10
- 239000002184 metal Substances 0.000 claims abstract description 161
- 229910052751 metal Inorganic materials 0.000 claims abstract description 161
- 238000006243 chemical reaction Methods 0.000 claims abstract description 158
- 238000001704 evaporation Methods 0.000 claims abstract description 23
- 230000008020 evaporation Effects 0.000 claims abstract description 23
- 239000002994 raw material Substances 0.000 claims abstract description 19
- 238000009833 condensation Methods 0.000 claims abstract description 16
- 230000005494 condensation Effects 0.000 claims abstract description 16
- 239000010410 layer Substances 0.000 claims description 133
- 239000007789 gas Substances 0.000 claims description 49
- 238000009413 insulation Methods 0.000 claims description 22
- 239000007809 chemical reaction catalyst Substances 0.000 claims description 20
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 14
- 230000009471 action Effects 0.000 claims description 11
- 239000003054 catalyst Substances 0.000 claims description 10
- 238000005192 partition Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000011810 insulating material Substances 0.000 claims description 7
- 239000012495 reaction gas Substances 0.000 claims description 7
- 238000006722 reduction reaction Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 6
- 229910052802 copper Inorganic materials 0.000 claims description 6
- 239000010949 copper Substances 0.000 claims description 6
- 230000000149 penetrating effect Effects 0.000 claims description 6
- 239000006260 foam Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 230000003247 decreasing effect Effects 0.000 claims description 4
- 239000011229 interlayer Substances 0.000 claims description 3
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- 238000005728 strengthening Methods 0.000 abstract description 2
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- 238000005984 hydrogenation reaction Methods 0.000 description 3
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- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000003380 propellant Substances 0.000 description 2
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
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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
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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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
- B01J8/0285—Heating or cooling the reactor
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- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/12—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon dioxide with hydrogen
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Abstract
The invention discloses a Sabatier reactor for reducing carbon dioxide in Mars atmosphere and a method thereof. The metal porous medium layer with the porosity gradually reduced is arranged along the flowing direction of the raw material gas, and the gradient temperature field of continuous transition from the high-temperature area to the low-temperature area is constructed, so that the Sabatier reaction at high temperature and low temperature is considered, and the reaction rate and the conversion rate of the Sabatier reaction are synchronously improved. The invention constructs a composite heat exchange strengthening structure by using the flat-plate heat pipe and the metal porous medium layer, fully utilizes the evaporation and condensation circulation of working media in the flat-plate heat pipe and the good space heat conduction capability of the metal porous medium layer, and utilizes the atmospheric cold energy of mars to eliminate the reaction heat of the Sabatier reaction, thereby ensuring the reliable and stable operation of the Sabatier reactor. The invention does not need to be provided with additional cooling equipment, thereby greatly improving the adaptability of the Sabatier reactor to Mars environment.
Description
Technical Field
The invention relates to the technical field of Mars detection, in particular to a Sabatier reactor for carbon dioxide hydrogenation methanation on the surface of Mars and a method thereof.
Background
The in-situ preparation of the Mars propellant is a key technology for realizing extraterrestrial activities such as extraterrestrial manned detection and the like. The main component of the atmosphere on the surface of the spark is carbon dioxide which accounts for 95.32 percent of the total amount, and the propellant can be obtained through reduction reaction. Carbon dioxide reduction has multiple technical paths, multiple factors such as maturity, operability, economy, long-term stability and the like are comprehensively considered, and carbon dioxide hydromethanation (Sabatier reaction) becomes the current mainstream technology.
The Sabatier reaction is a strong exothermic process limited by thermodynamic equilibrium, and the normal operation of the reaction is seriously affected by the temperature rise caused by the aggregation of a large amount of reaction heat, so that not only can the sintering and inactivation of a catalyst be caused and the reaction conversion rate be reduced, but also the reaction product can be changed along with the change of the reaction temperature to form a byproduct. To increase the Sabatier reaction rate, the reactor must be maintained at a high temperature, while to increase the conversion requires a lower temperature, depending on the Sabatier reaction characteristics. The key to the design of the Sabatier reactor is to adapt the structural characteristics of the reactor to the characteristics of the reaction, taking into account the differential requirements of reaction rate and conversion rate with respect to temperature. The prior Sabatier reactor structure usually arranges a heater at the front end, and cools the back end directly through a sleeve type structure. The structure has two defects, namely, a high-temperature area for improving the reaction rate is directly connected with a low-temperature area for improving the conversion rate, so that the high-temperature area and the low-temperature area are difficult to fully exert the set function, and the cooling efficiency of the sleeve type external cooling is limited, so that local hot spots are easily formed in the reactor when the reaction heat is quickly increased due to the increase of the flow rate of the raw material gas.
Disclosure of Invention
The invention aims to provide a Sabatier reactor for carbon dioxide hydrogenation methanation on the surface of Mars, which is characterized in that a flat heat pipe is coupled with foam metals with different porosities to construct a gradient temperature field, so that the reaction speed and the conversion rate of the Sabatier reaction are improved.
The invention aims to realize the purpose of the invention by the following technical scheme:
in a first aspect, the invention provides a Sabatier reactor for carbon dioxide hydromethanation on the surface of Mars, which comprises a heat-insulating reactor shell, wherein a reaction cavity inside the reactor shell is provided with an air inlet and an air outlet;
the reaction cavity is divided into a high-temperature reaction zone and a gradient temperature field reaction zone by an annular heat insulation partition plate;
a heater for heating the feed gas of the Sabatier reaction to the initial reaction temperature is arranged in the high-temperature reaction zone, and a Sabatier reaction catalyst is coated on the surface of the heater;
a first metal porous medium layer, a second metal porous medium layer and a third metal porous medium layer are sequentially arranged in the gradient temperature field reaction zone along the air inlet direction, the porosity of the first metal porous medium layer, the porosity of the second metal porous medium layer and the porosity of the third metal porous medium layer are decreased gradually, and Sabatier reaction catalysts are coated on the surfaces of the media; the three metal porous medium layers are subjected to heat exchange with external spark atmosphere through flat plate heat pipes penetrating through the reactor shell, so that Sabatier reaction heat in the three metal porous medium layers can be transferred to the spark atmosphere;
and after being introduced from the gas inlet, the raw material gas sequentially flows through the surface of the heater in the high-temperature reaction zone and the first metal porous medium layer, the second metal porous medium layer and the third metal porous medium layer in the gradient temperature field reaction zone and is discharged from the gas outlet.
Preferably, the reactor insulation shell is formed by nesting an outer Sabatier reactor shell and an inner Sabatier reactor shell inside and outside, and an insulation material is filled in an interlayer between the inner shell and the outer shell.
Preferably, the flat heat pipe comprises a flat heat pipe evaporation section, a flat heat pipe heat insulation section and a flat heat pipe condensation section which are connected in sequence, the flat heat pipe evaporation section is located in the gradient temperature field reaction zone and is connected with the first metal porous medium layer, the second metal porous medium layer and the third metal porous medium layer to form heat exchange contact, the flat heat pipe condensation section is located outside the reactor shell and contacts Mars atmosphere, the flat heat pipe penetrates through the reactor shell, and two ends of the flat heat pipe evaporation section and the two ends of the flat heat pipe condensation section are respectively connected with the flat heat insulation evaporation section and the flat heat pipe condensation section.
Preferably, the flat heat pipe is annularly arranged in the gradient temperature field reaction zone, and the evaporation section of the flat heat pipe is wrapped around the periphery of the three metal porous medium layers.
Preferably, the connection positions of the evaporation section of the flat-plate heat pipe and the first metal porous medium layer, the second metal porous medium layer and the third metal porous medium layer are filled with a heat conducting medium for eliminating thermal contact resistance.
Preferably, in the first aspect, the metal porous medium layers adopt copper foam as a metal framework, and the Sabatier reaction catalyst coated on the surface of the copper foam adopts a Ru-based catalyst.
In the first aspect, the heater preferably uses solar energy as a heat source.
Preferably, in the first aspect, the heat insulating material is a vacuum insulation panel.
Preferably, in the first aspect, three or more metal porous medium layers are sequentially arranged in the gradient temperature field reaction zone along the air inlet direction, and the porosity of each metal porous medium layer decreases progressively along the air inlet direction; the surfaces of all the metal porous medium layers are coated with Sabatier reaction catalysts and exchange heat with external spark atmosphere through flat plate type heat pipes penetrating through the reactor shell.
In a second aspect, the present invention provides a mars surface carbon dioxide hydromethanation method using a Sabatier reactor according to any one of the preceding aspects, which comprises:
introducing a raw material gas into a reaction cavity in the reactor shell from the gas inlet, firstly heating the raw material gas to a Sabatier reaction starting temperature in a high-temperature reaction zone through a heater, and thus, performing a reduction reaction under the action of a Sabatier reaction catalyst coated on the surface of the heater to convert part of the raw material gas into methane and water; then, continuously introducing the partially converted feed gas into a gradient temperature field reaction zone, sequentially flowing through a first metal porous medium layer, a second metal porous medium layer and a third metal porous medium layer with gradually reduced porosity, continuously performing three-stage conversion under the action of a Sabatier reaction catalyst coated on the surface of the medium and releasing reaction heat, and forming a temperature field with gradually reduced temperature along the airflow direction in the gradient temperature field reaction zone under the control of the porosity of the three metal porous medium layers so as to gradually improve the conversion rate of the feed gas; in the reaction process, the reaction heat in the first metal porous medium layer, the second metal porous medium layer and the third metal porous medium layer is transferred to the Mars atmosphere outside the reactor shell through the flat plate type heat pipe; and finally, collecting the reaction gas material after the conversion from the gas outlet.
Compared with the prior art, the invention has the outstanding and beneficial technical effects that:
according to the invention, the metal porous medium layer with the porosity gradually reduced is arranged along the flowing direction of the raw material gas, a gradient temperature field with continuous transition from a high-temperature area to a low-temperature area is constructed, the beneficial effects of high temperature and low temperature are maximized, and the reaction rate and the conversion rate of the Sabatier reaction are synchronously improved; the reaction heat of the Sabatier reaction is eliminated by fully utilizing the cold energy of the Mars atmosphere, no additional cooling equipment is required to be configured, and the adaptability of the Sabatier reactor to the Mars environment is greatly improved; the composite heat exchange strengthening structure is constructed by the flat-plate heat pipe and the metal porous medium layer, the evaporation and condensation circulation of working media in the flat-plate heat pipe and the good space heat conduction capability of the metal porous medium layer are fully utilized, and local hot spots possibly generated by the reactor are eliminated, so that the Sabatier reactor is ensured to operate reliably and stably.
The conception, the specific structure and the technical effects of the present invention will be further described with reference to the accompanying drawings so as to fully understand the objects, the features and the effects of the present invention.
Drawings
FIG. 1 is a schematic diagram of a Sabatier reactor for hydromethanation of carbon dioxide on the surface of Mars according to the invention.
In the figure: the device comprises a Sabatier reactor outer shell 1, a heat insulating material 2, a Sabatier reactor inner shell 3, a high-temperature reaction zone 4, a gradient temperature field reaction zone 5, a flat-plate heat pipe evaporation section 6, a flat-plate heat pipe heat insulating section 7, a flat-plate heat pipe condensation section 8, a heater 9, a heat insulating partition plate 10, a first metal porous medium layer 11, a second metal porous medium layer 12, a third metal porous medium layer 13 and a fixing module 14.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. The technical characteristics in the embodiments of the present invention can be combined correspondingly without mutual conflict.
In the description of the present invention, it should be understood that when an element is referred to as being "connected" to another element, it can be directly connected to the other element or be indirectly connected to the other element, i.e., intervening elements may be present. In contrast, when an element is referred to as being "directly connected" to another element, there are no intervening elements present.
In the description of the present invention, it is to be understood that the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implying any number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature.
Referring to fig. 1, in a preferred embodiment of the present invention, a Sabatier reactor for hydromethanation of carbon dioxide on a spark surface is provided, and its components include an outer Sabatier reactor shell 1, an insulating material 2, an inner Sabatier reactor shell 3, a high-temperature reaction region 4, a gradient temperature field reaction region 5, a flat heat pipe evaporation section 6, a flat heat insulation section 7, a flat heat pipe condensation section 8, a heater 9, an insulation partition plate 10, a first metal porous medium layer 11, a second metal porous medium layer 12, a third metal porous medium layer 13 and a fixing module 14. The Sabatier reactor is used for realizing the Sabatier reaction in the atmospheric environment on the surface of a spark, the raw material gas of the Sabatier reaction is carbon dioxide and hydrogen, the reaction temperature is about 450-800K, and the Sabatier reaction belongs to exothermic reaction. The reaction needs to be carried out under a catalyst, and Ru, ni, co, fe, mo and the like have better catalytic activity on the Sabatier reaction. The assembly and operation of the components of the Sabatier reactor are described in detail below.
Since the average temperature of the Martian atmosphere is about 216K and the minimum temperature is about 172K, and the Sabatier reaction needs to be started up at a high temperature, the reactor needs to be provided with an adiabatic reactor shell in order to eliminate the influence of the low-temperature Martian atmosphere on the reaction process. In this embodiment, the reactor insulation shell is formed by internally and externally nesting a Sabatier reactor outer shell 1 and a Sabatier reactor inner shell 3, and the interlayer of the inner and outer shells is filled with an insulating material 2. The outer shell 1 of the Sabatier reactor and the inner shell 3 of the Sabatier reactor can be made of metal materials or corrosion-resistant and ageing-resistant high polymer materials. The heat insulating material 2 may be a vacuum insulation panel. A reaction cavity is arranged in the reactor shell, and an air inlet and an air outlet which are communicated with the reaction cavity are formed in the shell. The reaction cavity is internally divided into a high-temperature reaction zone 4 and a gradient temperature field reaction zone 5, the middle of the reaction cavity is separated by a heat insulation partition plate 10, wherein the high-temperature reaction zone 4 is positioned on one side of an air inlet, and the gradient temperature field reaction zone 5 is positioned on one side of an air outlet. The heat insulation partition plate 10 is an annular plate body with a central opening, the high-temperature reaction zone 4 and the gradient temperature field reaction zone 5 are communicated through the central opening of the heat insulation partition plate 10, and due to the existence of the heat insulation partition plate 10, certain separability is kept, and direct heat exchange of the two reaction zones is reduced.
The high temperature reaction zone 4 is provided with a heater 9 for heating the feed gas for Sabatier reaction to the initial reaction temperature, and the heater 9 is coated with a Sabatier reaction catalyst on the surface. The heater 9 is used for heating the raw material gas to an initial reaction temperature, and the specific initial reaction temperature is determined according to the selected Sabatier reaction catalyst. The Sabatier reaction generally does not require reheating after it is initiated and can be maintained at reaction temperature by its own exotherm. The Sabatier reaction herein has a higher reaction rate for the entire reaction chamber due to the higher temperature of the high temperature reaction zone 4. However, the conversion rate of the reaction is reduced due to the over-high temperature, so that the reaction conversion rate needs to be increased by arranging the gradient temperature field reaction zone 5 subsequently.
Since the sun shine in the mars is sufficient, the heater 9 may be a heater using solar energy as a heat source. Of course, the electric energy can be stored in a wind energy and solar energy power generation mode and then heated by the electric energy, so that the phenomenon that the reaction cannot be started when no sunlight exists is avoided.
A first metal porous medium layer 11, a second metal porous medium layer 12 and a third metal porous medium layer 13 are sequentially arranged in the gradient temperature field reaction zone 5 along the air inlet direction, and the porosity of the first metal porous medium layer 11, the porosity of the second metal porous medium layer 12 and the porosity of the third metal porous medium layer 13 are decreased progressively. The first metal porous medium layer 11, the second metal porous medium layer 12 and the third metal porous medium layer 13 are sequentially a high-porosity metal porous medium, a middle-porosity metal porous medium and a low-porosity metal porous medium, and the surfaces of the media are coated with a Sabatier reaction catalyst. And the first metal porous medium layer 11, the second metal porous medium layer 12 and the third metal porous medium layer 13 form heat exchange with external spark atmosphere through the flat heat pipe penetrating through the reactor shell, so that Sabatier reaction heat in the three metal porous medium layers can be transferred to the spark atmosphere. The first metal porous medium layer 11, the second metal porous medium layer 12, the third metal porous medium layer 13 and the flat heat pipe can be installed on the Sabatier reactor inner shell 3 through the fixing module 14, and the relative fixing of the spatial positions of the first metal porous medium layer, the second metal porous medium layer, the third metal porous medium layer and the flat heat pipe is kept.
In the first metal porous medium layer 11, the second metal porous medium layer 12 and the third metal porous medium layer 13, each metal porous medium layer uses a metal porous medium as a metal framework, and then a Sabatier reaction catalyst is attached to the surface of the metal framework, so that Sabatier reaction heat can be quickly transferred to a negative heat evaporation section of the flat heat pipe through the porous metal framework. The specific metal framework and the form of the catalyst are not limited. As a better implementation mode of the embodiment of the invention, each metal porous dielectric layer can adopt foamy copper with good heat conductivity and high melting point as a metal framework, and the Sabatier reaction catalyst coated on the surface of the foamy copper can adopt Ru-based catalyst which is beneficial to reducing the Sabatier reaction starting temperature. Since the space heat conduction capacity of the metal porous medium is increased along with the reduction of the porosity, the lower the porosity is, the higher the heat conduction capacity is, so that the more heat is dissipated through the flat plate type heat pipe, and the lower the temperature of the metal porous medium layer is. Therefore, the first metal porous medium layer 11, the second metal porous medium layer 12 and the third metal porous medium layer 13 can form a gradient temperature field with gradually reduced temperature along the flowing direction of the raw material gas, the reaction rate of the first metal porous medium layer 11, the second metal porous medium layer 12 and the third metal porous medium layer 13 is gradually reduced, but the conversion rate of the Sabatier reaction is gradually improved.
It should be noted that the specific porosity in the three metal porous dielectric layers is not limited, and the three metal porous dielectric layers can meet the requirement of gradually decreasing the porosity, and the respective specific porosity can be optimally designed according to the actual reaction condition.
It should be noted that the specific form of the flat heat pipe is not limited, and the advantage of using such a heat pipe is that it can be tightly attached to the outer peripheral surface of each metal porous medium layer, so as to improve the heat transfer efficiency. Referring to fig. 1, as a preferred implementation manner of the embodiment of the present invention, the flat heat pipe includes a flat heat pipe evaporation section 6, a flat heat pipe insulation section 7, and a flat heat pipe condensation section 8, which are connected in sequence, the flat heat pipe evaporation section 6 is located in the gradient temperature field reaction region 5, and is connected to the first metal porous medium layer 11, the second metal porous medium layer 12, and the third metal porous medium layer 13 to form a heat exchange contact, the flat heat pipe condensation section 8 is located outside the reactor shell and contacts the mars atmosphere, the flat heat pipe insulation section 7 penetrates through the reactor shell, and two ends of the flat heat pipe evaporation section 6 and the flat heat pipe condensation section 8 are connected to each other. In a preferred implementation, the flat-plate heat pipe may be composed of a series of axial small heat pipes independent and parallel to each other, and each of the small heat pipes uses an axial micro-channel structure as a wick.
Furthermore, in order to increase the heat exchange area between the flat-plate heat pipe and the metal porous medium layer, the flat-plate heat pipe can be annularly arranged in the gradient temperature field reaction zone 5, and the evaporation section 6 of the flat-plate heat pipe is wrapped around the periphery of the three metal porous medium layers, so that the reaction heat is rapidly dissipated into the Mars atmosphere. Meanwhile, the connection positions of the flat-plate heat pipe evaporation section 6 and the first metal porous medium layer 11, the second metal porous medium layer 12 and the third metal porous medium layer 13 can be filled with heat-conducting media for eliminating thermal contact resistance.
In the actual reaction process, the raw material gas flows through the surface of the heater 9 in the high temperature reaction zone 4, the first metal porous medium layer 11, the second metal porous medium layer 12 and the third metal porous medium layer 13 in the gradient temperature field reaction zone 5 in sequence after being introduced from the gas inlet, and then is discharged from the gas outlet. In the process, the raw material gas firstly enters the high-temperature reaction zone 4, is heated by the heater 9, the temperature is raised to the reaction starting temperature, and then the reduction reaction is carried out under the action of the catalyst coated on the surface of the heater 9 to generate methane and water, wherein the Sabatier reaction rate is higher, but the conversion rate of the raw material gas is lower. Then, the partially converted raw gas enters a gradient temperature field reaction zone 5, firstly, the partially converted raw gas is contacted with the high-porosity metal porous medium 11, the raw gas is continuously converted and reaction heat is released under the action of a metal framework surface catalyst, and the temperature of a region where the high-porosity metal porous medium 11 is located is higher due to higher porosity; then, the porous medium is contacted with the intermediate porosity metal porous medium 12, the feed gas is continuously converted and releases reaction heat under the action of the metal framework surface catalyst, and the temperature of the area where the intermediate porosity metal porous medium 12 is located is continuously reduced due to moderate porosity; and finally, the low-porosity metal porous medium 13 is contacted, the feed gas is continuously converted and reaction heat is released under the action of the metal framework surface catalyst, and the temperature of the area where the low-porosity metal porous medium 13 is located is lower due to lower porosity. The regions of the high-porosity metal porous medium 11, the intermediate-porosity metal porous medium 12 and the low-porosity metal porous medium 13 form a temperature field with gradually reduced temperature, so that high-efficiency transition from high reaction rate to high conversion rate can be completed. And the porous metal medium 11 with porosity, the porous metal medium 12 with middle porosity and the porous metal medium 13 with low porosity transfer the Sabatier reaction heat to the evaporation section 6 of the flat heat pipe, the medium in the flat heat pipe is vaporized after absorbing heat, enters the condensation section 8 of the flat heat pipe through the heat insulation section 7 of the flat heat pipe, absorbs the cold energy of the atmosphere of Mars to complete liquefaction, and finally returns to the evaporation section 6 of the flat heat pipe under the action of the liquid absorption core.
In addition, three metal porous medium layers are arranged in the reaction cavity of the Sabatier reactor, but three layers are not necessarily required. In other embodiments of the present invention, more than three metal porous medium layers may be sequentially disposed in the gradient temperature field reaction region 5 along the air inlet direction, that is, a metal porous medium layer may be further added outside the first metal porous medium layer 11, the second metal porous medium layer 12, and the third metal porous medium layer 13, so as to improve the continuity from the high temperature region to the low temperature region. Similar to the method of adopting three layers of metal porous medium layers, the porosity of each metal porous medium layer in the air inlet direction needs to be kept gradually reduced, sabatier reaction catalysts are coated on the surfaces of all the metal porous medium layers, and the metal porous medium layers need to exchange heat with the external Martian atmosphere through flat plate type heat pipes penetrating through the reactor shell.
In addition, based on the Sabatier reactor for Mars surface carbon dioxide hydromethanation, the invention can further provide a Mars surface carbon dioxide hydromethanation method, which comprises the following specific steps:
introducing a raw material gas into a reaction cavity in the reactor shell from the gas inlet, firstly heating the raw material gas to a Sabatier reaction starting temperature in a high-temperature reaction zone 4 through a heater 9, so that a reduction reaction is carried out under the action of a Sabatier reaction catalyst coated on the surface of the heater 9, and part of the raw material gas is converted into methane and water; then, continuously introducing the partially converted feed gas into the gradient temperature field reaction zone 5, sequentially flowing through a first metal porous medium layer 11, a second metal porous medium layer 12 and a third metal porous medium layer 13 with gradually reduced porosity, continuously performing three-stage conversion under the action of a Sabatier reaction catalyst coated on the surface of the medium and releasing reaction heat, and forming a temperature field with gradually reduced temperature along the airflow direction in the gradient temperature field reaction zone 5 under the control of the porosity of the three metal porous medium layers, thereby gradually improving the conversion rate of the feed gas; in the reaction process, the reaction heat in the first metal porous medium layer 11, the second metal porous medium layer 12 and the third metal porous medium layer 13 is transferred to the spark atmosphere outside the reactor shell through the flat-plate heat pipe; and finally, collecting the reaction gas material after the conversion from the gas outlet.
In the invention, if the reaction is complete, the reaction gas material after final conversion is the mixed gas of methane and water, but if the reaction is incomplete, the reaction gas material after final conversion contains carbon dioxide, hydrogen, methane and water. The mixed gas can be separated according to the subsequent use requirement, so that separate methane and water can be obtained. The separation of each component in the reaction gas can be realized by utilizing the difference of condensation points among the components, the temperature of the reaction gas is gradually reduced, each component is gradually condensed into a liquid phase, and the liquid phase is separated from a gas phase through centrifugal separation, so that each component is respectively obtained.
The above-described embodiments are merely preferred embodiments of the present invention, which should not be construed as limiting the invention. Various changes and modifications may be made by one of ordinary skill in the pertinent art without departing from the spirit and scope of the present invention. Therefore, the technical scheme obtained by adopting the mode of equivalent replacement or equivalent transformation is within the protection scope of the invention.
Claims (10)
1. A Sabatier reactor for hydromethanation of carbon dioxide on the surface of Mars is characterized by comprising a heat-insulating reactor shell, wherein a reaction cavity in the reactor shell is provided with an air inlet and an air outlet;
the reaction cavity is divided into a high-temperature reaction zone (4) and a gradient temperature field reaction zone (5) by an annular heat insulation partition plate (10);
a heater (9) for heating the feed gas of the Sabatier reaction to the initial reaction temperature is arranged in the high-temperature reaction zone (4), and a Sabatier reaction catalyst is coated on the surface of the heater (9);
a first metal porous medium layer (11), a second metal porous medium layer (12) and a third metal porous medium layer (13) are sequentially arranged in the gradient temperature field reaction zone (5) along the air inlet direction, the porosity of the first metal porous medium layer (11), the porosity of the second metal porous medium layer (12) and the porosity of the third metal porous medium layer (13) are decreased gradually, and the surface of each medium is coated with a Sabatier reaction catalyst; the three metal porous medium layers are subjected to heat exchange with external spark atmosphere through flat plate heat pipes penetrating through the reactor shell, so that Sabatier reaction heat in the three metal porous medium layers can be transferred to the spark atmosphere;
and after being introduced from the gas inlet, the raw gas flows through the surface of the heater (9) in the high-temperature reaction zone (4) and the first metal porous medium layer (11), the second metal porous medium layer (12) and the third metal porous medium layer (13) in the gradient temperature field reaction zone (5) in sequence and is discharged from the gas outlet.
2. The Sabatier reactor for the hydromethanation of Mars surface carbon dioxide according to claim 1, characterized in that the reactor insulation shell is formed by internally and externally nesting a Sabatier reactor outer shell (1) and a Sabatier reactor inner shell (3), and the inner shell and the outer shell interlayer are filled with an insulating material (2).
3. The Sabatier reactor for hydromethanation of carbon dioxide on a Mars surface according to claim 2, wherein the flat heat pipe comprises a flat heat pipe evaporation section (6), a flat heat pipe insulation section (7) and a flat heat pipe condensation section (8) which are sequentially connected, the flat heat pipe evaporation section (6) is positioned in the gradient temperature field reaction zone (5), is connected with the first metal porous medium layer (11), the second metal porous medium layer (12) and the third metal porous medium layer (13) and forms heat exchange contact, the flat heat pipe condensation section (8) is positioned outside the reactor shell and contacts Mars atmosphere, the flat heat pipe insulation section (7) penetrates through the reactor shell, and two ends of the flat heat pipe insulation section are respectively connected with the flat heat pipe evaporation section (6) and the flat heat pipe condensation section (8).
4. The Sabatier reactor for Mars surface carbon dioxide hydromethanation according to claim 3, wherein the flat-plate heat pipe is annularly arranged in the gradient temperature field reaction zone (5), and the evaporation section (6) of the flat-plate heat pipe is wrapped around the periphery of the three metal porous medium layers.
5. The Sabatier reactor for carbon dioxide hydromethanation on Mars surface according to claim 2, wherein the connecting positions of the flat-plate heat pipe evaporation section (6) and the first metal porous medium layer (11), the second metal porous medium layer (12) and the third metal porous medium layer (13) are filled with a heat-conducting medium for eliminating contact thermal resistance.
6. The Sabatier reactor for hydromethanation of carbon dioxide on the surface of mars according to claim 1, wherein each metal porous dielectric layer adopts copper foam as a metal framework, and the Sabatier reaction catalyst coated on the surface of the copper foam adopts a Ru-based catalyst.
7. The Sabatier reactor for the hydromethanation of Mars surface carbon dioxide according to claim 1, characterized in that the heater (9) uses solar energy as the heat source.
8. The Sabatier reactor for the hydromethanation of Mars surface carbon dioxide according to claim 1, characterized in that the thermally insulating material (2) is a vacuum insulation panel.
9. The Sabatier reactor for hydromethanation of carbon dioxide on the surface of mars according to claim 1, wherein more than three layers of metal porous medium layers are sequentially arranged in the gradient temperature field reaction zone (5) along the air inlet direction, and the porosity of each metal porous medium layer along the air inlet direction is gradually reduced; sabatier reaction catalysts are coated on the surfaces of all the metal porous medium layers, and heat exchange is formed between the metal porous medium layers and the external spark atmosphere through flat plate type heat pipes penetrating through the reactor shell.
10. A mars surface carbon dioxide hydromethanation process using a Sabatier reactor according to any one of claims 1 to 9, which comprises:
introducing a raw material gas into a reaction cavity in the reactor shell from the gas inlet, firstly heating the raw material gas to a Sabatier reaction starting temperature in a high-temperature reaction zone (4) through a heater (9), and thus, performing a reduction reaction under the action of a Sabatier reaction catalyst coated on the surface of the heater (9) to convert part of the raw material gas into methane and water; then, continuously introducing the partially converted feed gas into a gradient temperature field reaction zone (5), sequentially flowing through a first metal porous medium layer (11), a second metal porous medium layer (12) and a third metal porous medium layer (13) with gradually reduced porosity, continuously performing three-stage conversion under the action of a Sabatier reaction catalyst coated on the surface of the medium and releasing reaction heat, and forming a temperature field with gradually reduced temperature along the gas flow direction in the gradient temperature field reaction zone (5) under the control of the porosity of the three metal porous medium layers so as to gradually improve the conversion rate of the feed gas; in the reaction process, reaction heat in the first metal porous medium layer (11), the second metal porous medium layer (12) and the third metal porous medium layer (13) is transferred to Mars atmosphere outside the reactor shell through the flat plate type heat pipe; and finally, collecting the reaction gas material after the conversion from the gas outlet.
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