CN112755923A - Self-heating type reactor for preparing methane by catalytic hydrogenation of carbon dioxide - Google Patents
Self-heating type reactor for preparing methane by catalytic hydrogenation of carbon dioxide Download PDFInfo
- Publication number
- CN112755923A CN112755923A CN202011434050.2A CN202011434050A CN112755923A CN 112755923 A CN112755923 A CN 112755923A CN 202011434050 A CN202011434050 A CN 202011434050A CN 112755923 A CN112755923 A CN 112755923A
- Authority
- CN
- China
- Prior art keywords
- sealing plate
- shell
- reaction
- carbon dioxide
- catalytic hydrogenation
- 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.)
- Pending
Links
Images
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
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- 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
-
- 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
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a self-heating reactor for preparing methane by catalytic hydrogenation of carbon dioxide, which comprises: the inner space of the cylindrical tubular shell is divided into three mutually isolated spaces by an upper sealing plate and a lower sealing plate which are parallel to each other; a plurality of parallel reaction tubes are arranged in the reaction section of the tubular shell, the upper ends of tube passes of the reaction tubes are communicated with the upper sealing section through corresponding through holes of the upper sealing plate, and the lower ends of the tube passes of the reaction tubes are communicated with the lower sealing section through corresponding through holes of the lower sealing plate; filling a solid catalyst in the reaction tube; the upper sealing plate and the lower sealing plate respectively seal the gap between the tubular shell and the reaction tube, so that the gap between the tubular shell and the reaction tube forms a shell pass; the lower part of the reaction section of the tubular shell is provided with a raw material gas inlet which is communicated with the shell pass; the upper sealing plate is covered with a plurality of vent holes at the part of the shell pass; and a discharge hole is formed in the lower sealing section shell. The invention has simple structure and convenient operation, realizes the purpose of preheating the reaction raw material by using the methanation reaction heat, and can effectively reduce the energy consumption and the operation cost of the system.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a self-heating type reactor for preparing methane by catalytic hydrogenation of carbon dioxide.
Background
At present, the emission of greenhouse gases represented by carbon dioxide causes various problems such as global warming, glacier thawing, sea level rising and the like. At the same time, the large amount of carbon dioxide also poses a serious challenge to global agricultural production and ecosystems. The problem of carbon dioxide emission reduction has become a common topic in various countries in the world.
On the other hand, due to the unbalanced distribution of natural resources, renewable energy resources such as photoelectricity, wind power, hydropower and the like are abundant in areas represented by the Chinese and western parts of China, but the economic development is relatively lagged behind, and the phenomena of ' light abandonment ', wind abandonment ' and the like are caused by surplus electric power. Methane is the main component of natural gas, is also an important fuel, and can be delivered to various end users through a natural gas pipeline network. The electrical gas (PtG) technology is receiving increasing attention to convert excess electricity to methane through electrolytic hydrogen production and carbon dioxide hydromethanation processes.
The core equipment in the carbon dioxide hydromethanation process is a methanation reactor. Chinese patent document CN110354765A discloses a photothermal fixed bed reaction experimental device and method for carbon dioxide hydrogenation methanation reaction, wherein the upper surface, the lower surface, the front surface and the rear surface of a reaction box body are respectively provided with a xenon lamp and a reflector, and the four lamp tubes can make the temperature of a catalyst bed layer more uniform, but the reactor is complex in design and difficult to industrially apply. Chinese patent document CN103752227A discloses a methanation reactor with two shells, an inner shell and an outer shell, but the heat exchange area between the two shells is limited, and the heat exchange effect is poor. Chinese patent document CN107224940A discloses a radial fixed bed methanation reactor, which uses the reaction heat to produce by-product steam, but the reactor has problems of complicated design and low utilization efficiency of the reaction heat. Chinese patent document CN103920429A discloses an axial fixed bed methanation reactor, but does not fully utilize the heat of methanation reaction, resulting in energy loss.
Disclosure of Invention
The invention aims to provide an autothermal carbon dioxide catalytic hydrogenation methane preparation reactor, which can preheat reaction raw materials by using methanation reaction heat in situ and reduce system energy consumption so as to solve the problems of complex design, poor heat exchange effect, low reaction heat utilization efficiency and the like in the prior art.
In order to achieve the purpose, the technical scheme of the invention is as follows:
an autothermal carbon dioxide catalytic hydrogenation methane production reactor comprising: the inner space of the cylindrical tubular shell is divided into three mutually isolated spaces by an upper sealing plate and a lower sealing plate which are parallel to each other, the upper part of the upper sealing plate is provided with an upper sealing section, a reaction section is arranged between the upper sealing plate and the lower sealing plate, and the lower part of the lower sealing plate is provided with a lower sealing section; a plurality of parallel reaction tubes are arranged in the reaction section of the tubular shell, the upper ends of tube passes of the reaction tubes are communicated with the upper sealing section through corresponding through holes of the upper sealing plate, and the lower ends of the tube passes of the reaction tubes are communicated with the lower sealing section through corresponding through holes of the lower sealing plate; solid catalysts are filled in the reaction tubes, and different filling modes are selected according to different forms of catalysts on the market; the reaction tube is characterized in that the upper sealing plate and the lower sealing plate respectively seal gaps between the tubular shell and the reaction tube, so that the gaps between the tubular shell and the reaction tube form a shell pass; the lower part of the reaction section of the tubular shell is provided with a raw material gas inlet which is communicated with the shell pass; the upper sealing plate covers the part of the shell pass and is provided with a plurality of vent holes which are used as gas outlets of the shell pass; and a discharge port is arranged on the lower sealing section shell, and the material after the reaction in the reaction tube is finished enters the lower sealing section and is discharged from the discharge port.
Furthermore, a reinforced heat exchange mechanism is arranged in the shell pass of the tubular shell, and the reinforced heat exchange mechanism is at least one of a baffle plate, random packing and structured packing and is used for prolonging the retention time of the feed gas and better performing heat exchange.
Furthermore, the horizontal position of the feed gas inlet is close to the lower sealing plate, so that the full utilization of reaction heat is facilitated.
Further, the length-diameter ratio of the tubular shell is 0.5-150; the inner diameter of the reaction tube is 10 mm-100 mm, and the number of the reaction tubes is 3-5000 generally.
Further, the arrangement of the reaction tubes on the upper and lower sealing plates includes, but is not limited to, one of regular triangle, square straight line and square staggered arrangement.
Furthermore, the aperture ratio of the vent hole on the upper sealing plate is 1-60%.
Further, the shape of the lower seal segment shell and the upper seal segment shell is one of an ellipse, a hemisphere and a flat plate; and a thermometer and an exhaust valve are arranged at the top of the upper sealing section shell and used for discharging unreacted gas during pressure relief or production stop.
Compared with the prior art, the invention has the following advantages:
the invention has simple structure and convenient operation, realizes the purpose of preheating the reaction raw material by using methanation reaction heat through material heat exchange between the tube side and the shell side of the reactor, saves the energy consumption required by preheating the reaction raw material, simultaneously saves the cooling energy consumption required by removing the reaction heat, and can effectively reduce the system energy consumption and the operation cost.
Drawings
FIG. 1 is a schematic structural view of the present invention;
in the figure: the method comprises the following steps of 1-tubular shell, 2-reaction tube, 3-catalyst bed, 4-shell pass, 5-upper sealing plate, 6-lower sealing plate, 7-raw material gas inlet, 8-discharge port, 9-lower sealing section shell, 10-upper sealing section shell and 11-vent hole.
Detailed Description
It should be understood by those skilled in the art that the present embodiment is only for illustrating the present invention and is not to be used as a limitation of the present invention, and changes and modifications of the embodiment can be made within the scope of the claims of the present invention.
As shown in fig. 1. An autothermal carbon dioxide catalytic hydrogenation methane production reactor comprising: the inner space of the cylindrical tubular shell 1 is divided into three mutually isolated spaces by an upper seal plate 5 and a lower seal plate 6 which are parallel to each other, the upper part of the upper seal plate 5 is an upper seal section, a reaction section is arranged between the upper seal plate 5 and the lower seal plate 6, and the lower part of the lower seal plate 6 is a lower seal section; a plurality of parallel reaction tubes 2 are arranged in the reaction section of the tubular shell 1, the upper ends of tube passes of the reaction tubes are communicated with the upper sealing section through corresponding through holes of the upper sealing plate 5, and the lower ends of the tube passes of the reaction tubes are communicated with the lower sealing section through corresponding through holes of the lower sealing plate 6; the reaction tube 2 is filled with a solid catalyst 3, and different filling modes are selected according to different forms of catalysts on the market; the upper sealing plate 5 and the lower sealing plate 6 respectively seal the gap between the tubular shell 1 and the reaction tube 2, so that the gap between the four forms a shell pass 4; the lower part of the reaction section of the tubular shell 1 is provided with a raw material gas inlet 7 communicated with the shell pass 4; the part of the upper sealing plate 5, which covers the shell pass 4, is provided with a plurality of vent holes 11 which are used as gas outlets of the shell pass 4; and a discharge port 8 is formed in the lower sealing section shell 9, and materials after the reaction in the reaction tube 2 is completed enter the lower sealing section and are discharged from the discharge port 8.
Furthermore, a reinforced heat exchange mechanism is arranged in the shell pass 4 of the tubular shell 1, and the reinforced heat exchange mechanism is at least one of a baffle plate, random packing and structured packing and is used for prolonging the retention time of the feed gas and better performing heat exchange.
Furthermore, the horizontal position of the feed gas inlet 7 is close to the lower sealing plate 6, which is beneficial to the full utilization of reaction heat.
Further, the length-diameter ratio of the tubular shell 1 is 0.5-150; the inner diameter of the reaction tube 2 is 10 mm-100 mm, and the number of the reaction tubes is 3-5000 generally.
Further, the arrangement of the reaction tubes 2 on the upper and lower closure plates 5 and 6 includes, but is not limited to, regular triangle, square straight line, and square staggered arrangement.
Further, the aperture ratio of the vent hole 11 on the upper sealing plate 5 is 1% to 60%.
Further, the shapes of the lower seal section shell 9 and the upper seal section shell 10 include but are not limited to an ellipse, a hemisphere and a flat plate; a thermometer and an exhaust valve are arranged at the top of the upper sealing section shell 10, and the exhaust valve is used for discharging unreacted gas during pressure relief or production stop.
Example 1
A plant utilizes an autothermal carbon dioxide catalytic hydrogenation methane production reactor as shown in figure 1: the reactors are 2 in parallel connection; the tubular shell 1 is cylindrical, and the length-diameter ratio is 20; 80 reaction tubes 2 in a single reactor are provided, and the inner diameter is 20 mm; the arrangement mode of the reaction tubes 2 on the upper sealing plate 5 and the lower sealing plate 6 is regular triangle, and the aperture ratio of the vent holes 11 on the upper sealing plate 5 is 20%; the lower sealing section shell 9 and the upper sealing section shell 10 are elliptical sealing heads; a spiral baffle plate is arranged in the shell pass 4 to strengthen the heat exchange between the tube pass and the shell pass.
The raw material gas firstly enters the shell pass 4 between the tubular shell 1 and the reaction tube 2, is heated by the reaction tube 2, then enters the upper sealing section shell 10 through the vent hole 11, and then enters the tube pass catalyst of the reaction tube 2 to generate methanation reaction, and the shell pass 4 and the reaction tube pass have opposite material flowing directions, so that the purpose of preheating the raw material gas by utilizing the methanation reaction heat is realized. The feed gas of example 1 was preheated to 200 ℃ and the heat utilization rate of methanation was 73%.
Example 2
A plant utilizes an autothermal carbon dioxide catalytic hydrogenation methane production reactor as shown in figure 1: a single reactor is adopted, the tubular shell 1 is cylindrical, and the length-diameter ratio is 10; 150 reaction tubes 2 in the reactor have the inner diameter of 30 mm; the reaction tubes 2 are arranged on the upper sealing plate 5 and the lower sealing plate 6 in a staggered square mode, and the aperture ratio of the vent holes 11 on the upper sealing plate 5 is 12%; the lower sealing section shell 9 and the upper sealing section shell 10 are hemispherical end sockets; regular packing is arranged in the shell pass 4 to strengthen the heat exchange between the tube pass and the shell pass.
The raw material gas firstly enters the shell pass 4 between the tubular shell 1 and the reaction tube 2, is heated by the reaction tube 2, then enters the upper sealing section shell 10 through the vent hole 11, and then enters the tube pass catalyst of the reaction tube 2 to generate methanation reaction, and the shell pass 4 and the reaction tube pass have opposite material flowing directions, so that the purpose of preheating the raw material gas by utilizing the methanation reaction heat is realized. The feed gas of example 2 was preheated to 250 ℃ and the heat utilization rate of methanation was 80%.
Claims (9)
1. An autothermal carbon dioxide catalytic hydrogenation methane production reactor comprising: the inner space of the cylindrical tubular shell (1) is divided into three mutually isolated spaces by an upper sealing plate (5) and a lower sealing plate (6) which are parallel to each other, the upper part of the upper sealing plate (5) is provided with an upper sealing section, a reaction section is arranged between the upper sealing plate (5) and the lower sealing plate (6), and the lower part of the lower sealing plate (6) is provided with a lower sealing section; a plurality of parallel reaction tubes (2) are arranged in the reaction section of the tubular shell (1), the upper ends of tube passes of the reaction tubes are communicated with the upper sealing section through corresponding through holes of the upper sealing plate (5), and the lower ends of the tube passes of the reaction tubes are communicated with the lower sealing section through corresponding through holes of the lower sealing plate (6); the reaction tube (2) is filled with a solid catalyst (3);
the reaction tube is characterized in that the upper sealing plate (5) and the lower sealing plate (6) respectively seal off a gap between the tubular shell (1) and the reaction tube (2), so that the gap between the four gaps forms a shell pass (4); the lower part of the reaction section of the tubular shell (1) is provided with a raw material gas inlet (7) communicated with the shell pass (4); the part of the upper sealing plate (5) covering the shell pass (4) is provided with a plurality of vent holes (11); and a discharge hole (8) is formed in the lower sealing section shell (9).
2. The reactor for preparing methane by catalytic hydrogenation of carbon dioxide in an autothermal form of claim 1, wherein a heat exchange enhancement mechanism is arranged in the shell pass (4) of the tubular shell (1), and the heat exchange enhancement mechanism is at least one of a baffle plate, random packing and structured packing.
3. The reactor for methane production by catalytic hydrogenation of carbon dioxide according to claim 1, wherein the feed gas inlet (7) is positioned horizontally next to the lower closing plate (6).
4. The reactor for preparing methane by catalytic hydrogenation of carbon dioxide in an autothermal form of claim 1, wherein the length to diameter ratio of the tubular shell (1) is 0.5-150.
5. The reactor for preparing methane by catalytic hydrogenation of carbon dioxide in an autothermal form according to claim 1, wherein the reaction tubes (2) have an inner diameter of 10 to 100mm and a number of 3 to 5000.
6. The reactor for methane production through catalytic hydrogenation of carbon dioxide with self-heating type according to claim 1, wherein the arrangement of the reaction tubes (2) on the upper sealing plate (5) and the lower sealing plate (6) is one of regular triangle, square straight line and square staggered.
7. The reactor for methane production by catalytic hydrogenation of carbon dioxide according to claim 1, wherein the vent holes (11) have an opening ratio of 1% to 60% in the upper sealing plate (5).
8. The reactor for methane production by catalytic hydrogenation of carbon dioxide with self-heating according to claim 1, wherein the lower seal segment shell (9) and the upper seal segment shell (10) have one of an oval shape, a hemispherical shape and a flat plate shape.
9. The reactor for methane production by catalytic hydrogenation of carbon dioxide with self-heating according to claim 8, wherein a thermometer and a vent valve are provided on the top of the upper block shell (10).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011434050.2A CN112755923A (en) | 2020-12-10 | 2020-12-10 | Self-heating type reactor for preparing methane by catalytic hydrogenation of carbon dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011434050.2A CN112755923A (en) | 2020-12-10 | 2020-12-10 | Self-heating type reactor for preparing methane by catalytic hydrogenation of carbon dioxide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112755923A true CN112755923A (en) | 2021-05-07 |
Family
ID=75693510
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011434050.2A Pending CN112755923A (en) | 2020-12-10 | 2020-12-10 | Self-heating type reactor for preparing methane by catalytic hydrogenation of carbon dioxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112755923A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114307908A (en) * | 2022-01-19 | 2022-04-12 | 华中科技大学 | Device and method for synthesizing liquid fuel through carbon dioxide multi-field concerted catalytic hydrogenation |
| WO2024180920A1 (en) * | 2023-02-28 | 2024-09-06 | 日本特殊陶業株式会社 | Reactor |
-
2020
- 2020-12-10 CN CN202011434050.2A patent/CN112755923A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114307908A (en) * | 2022-01-19 | 2022-04-12 | 华中科技大学 | Device and method for synthesizing liquid fuel through carbon dioxide multi-field concerted catalytic hydrogenation |
| WO2024180920A1 (en) * | 2023-02-28 | 2024-09-06 | 日本特殊陶業株式会社 | Reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112755923A (en) | Self-heating type reactor for preparing methane by catalytic hydrogenation of carbon dioxide | |
| CN104118848B (en) | A kind of hydrogen production from methanol-steam reforming reaction unit | |
| CN110357039B (en) | Biogas and solar complementary synthesis gas preparation system and method | |
| CN112892460B (en) | Self-heating methanol reforming hydrogen production reactor | |
| CN210103451U (en) | Miniature methane reforming hydrogen production device | |
| CN201519571U (en) | Shell and tube reactor for producing chloroethylene by utilizing acetylene method | |
| CN202737041U (en) | Natural gas steam reforming hydrogen production device for micro fuel cells | |
| CN212328238U (en) | Novel sulfuric acid decomposition device for thermochemical sulfur-iodine cycle hydrogen production | |
| CN215028705U (en) | Self-heating type reactor for preparing methane by catalytic hydrogenation of carbon dioxide | |
| CN212559452U (en) | Biological methane hydrogen production equipment | |
| CN110875711B (en) | Fuel preparation system and method based on photovoltaic and solid oxide fuel cell | |
| CN101551163A (en) | Solar heat-collecting core, heat collector and water heater | |
| CN111256375A (en) | Heat transfer pipe for molten salt fluid and heat absorber thereof | |
| US9433911B2 (en) | Reactor with honeycomb catalyst for fuel reformation | |
| CN212503986U (en) | Multi-return-stroke reforming hydrogen production reactor | |
| CN212559457U (en) | Integrated high-performance reforming reactor | |
| CN104830350A (en) | Biomass organic carbon preparation device | |
| CN201662066U (en) | Catalytic burner using exhaust gas generated by hydrogen production as heat source | |
| CN113912008A (en) | Pressure swing adsorption hydrogen production method for coke oven gas | |
| CN211035229U (en) | Reaction material input mechanism matched with integrated reforming hydrogen production device | |
| CN215049772U (en) | Modular device for producing methane by catalytic hydrogenation of carbon dioxide | |
| CN202752010U (en) | Gas phase hydrogenation reactor | |
| CN210656144U (en) | Tail gas heating type reformer for producing hydrogen from methanol | |
| CN214360254U (en) | Natural gas reformer | |
| CN221753322U (en) | Reforming reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |