CN114804027A - Reaction device for methane autothermal reforming porous medium - Google Patents
Reaction device for methane autothermal reforming porous medium Download PDFInfo
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- CN114804027A CN114804027A CN202210282828.5A CN202210282828A CN114804027A CN 114804027 A CN114804027 A CN 114804027A CN 202210282828 A CN202210282828 A CN 202210282828A CN 114804027 A CN114804027 A CN 114804027A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
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Abstract
The invention relates to a biogas autothermal reforming porous medium reaction device, which comprises a device shell, a porous medium reactor arranged in the device shell, a first air pipe and a second air pipe, wherein the first air pipe and the second air pipe are respectively connected with the device shell; a first space is arranged between the device shell and the porous medium reactor; the center of the porous medium reactor is provided with a high-temperature reaction zone formed by focusing thermal radiation; porous media are densely filled in the porous media reactor; the first space is communicated with the high-temperature reaction zone through a porous medium to form a reaction gas inner passage; the first air pipe, the reaction gas inner passage and the second air pipe are communicated in sequence. In the porous medium reactor, the flow cross section of the reaction gas is gradually changed, and the high temperature of the central high-temperature reaction area ensures continuous and efficient completion of the chemical reaction, so that the problem of carbon deposition of the catalyst in the traditional catalytic reforming reactor can be thoroughly solved, the continuous and efficient reaction of preparing the synthesis gas by autothermal reforming is realized, and the cost of preparing the synthesis gas by autothermal reforming is greatly reduced.
Description
Technical Field
The invention relates to the field of chemical reaction devices, in particular to a methane self-heating reforming porous medium reaction device.
Background
The technology of methane autothermal reforming, methane autothermal dry reforming, methane autothermal reforming and garbage landfill gas autothermal reforming for preparing synthesis gas has very important significance for efficiently utilizing biomass gas, reducing the emission of greenhouse gas and realizing the aim of carbon neutralization.
The invention can realize continuous and high-efficiency autothermal reforming reaction by utilizing the methane autothermal reforming porous medium reaction device under the condition of not using a catalyst, not only can thoroughly solve the problem of carbon deposition of the catalyst in the traditional catalytic reforming reactor, but also can realize continuous and high-efficiency autothermal reforming reaction for preparing synthesis gas under the condition of not needing to pretreat methane and landfill gas, and can greatly reduce the cost for preparing the synthesis gas by autothermal reforming.
Disclosure of Invention
Aiming at the technical problems in the prior art, the invention aims to: the methane autothermal reforming porous medium reaction device can realize efficient and continuous autothermal reforming reaction, thereby thoroughly solving the problem of carbon deposition of a catalyst in the traditional catalytic reforming reactor.
In order to achieve the purpose, the invention adopts the following technical scheme:
a biogas autothermal reforming porous medium reaction device comprises a device shell, a porous medium reactor arranged in the device shell, a first gas pipe and a second gas pipe which are respectively connected with the device shell;
a first space is arranged between the device shell and the porous medium reactor;
the center of the porous medium reactor is provided with a high-temperature reaction zone formed by focusing thermal radiation;
porous media are densely filled in the porous media reactor;
the first space is communicated with the high-temperature reaction zone through a porous medium to form a reaction gas inner passage;
the first air pipe, the reaction gas inner passage and the second air pipe are communicated in sequence.
Furthermore, the first air pipe and the second air pipe are mutually sleeved.
Furthermore, a heat exchanger is arranged outside the device shell, and two ends of the heat exchanger are respectively connected to the first air pipe and the second air pipe.
Furthermore, the first air pipe sequentially penetrates through one side of the device shell and the whole porous medium reactor and is connected to the first space, and the second air pipe sequentially penetrates through one side of the device shell and one side of the porous medium reactor and is connected to the high-temperature reaction area.
Furthermore, the first air pipe sequentially penetrates through one side of the device shell and one side of the porous medium reactor and is connected to the high-temperature reaction zone, and the second air pipe penetrates through one side of the device shell and is connected to the high-temperature reaction zone.
Further, first trachea and second trachea all locate device casing upside.
Further, the cross section of the reaction gas inner passage gradually changes along the reaction gas flow path.
Furthermore, the porous medium reactor is spherical, ellipsoidal, cylindrical or polyhedral, and the shape of the shell of the device is matched with that of the porous medium reactor.
Further, the porous medium is an inert porous medium, a catalyst or a mixture of the catalyst and the inert porous medium.
Further, the porous medium has one or more porosities.
In summary, the present invention has the following advantages:
(1) after the reaction gas mixture enters the second air pipe, the reaction gas mixture can be preheated by high-temperature gas in the first air pipe, so that the stable proceeding of the chemical reaction is facilitated, and meanwhile, the temperature of a central high-temperature area of the reactor can be increased, and the complete proceeding of the chemical reaction is facilitated.
(2) After the reaction gas mixture enters the porous medium reactor, because of the heat transfer characteristic of the porous medium reactor, super-adiabatic high temperature can be formed in the porous medium reactor, which is beneficial to the continuous and stable operation of the reforming reaction.
(3) The gas flows along the radius direction of the porous medium reactor, the flow cross section area is gradually changed, and the flame front is favorably stabilized in the porous medium.
(4) In the central area of the reaction device, a central high-temperature area is formed by the radiation of the wall surface of the surrounding porous medium reactor, which is beneficial to realizing high-efficiency autothermal reforming reaction.
(5) The gas pipe high-temperature section arranged in the high-temperature area in the cavity of the porous medium reaction device can prolong the retention time of gas in the high-temperature area, and is beneficial to complete reforming reaction.
(6) The methane or the landfill gas can be directly used without pretreatment, thereby greatly reducing the cost.
Drawings
Fig. 1 is a schematic structural view of embodiment 1.
FIG. 2 is a schematic diagram of the structure of a spherical porous medium reactor.
Fig. 3 is a schematic structural view of embodiment 2.
Fig. 4 is a schematic structural view of embodiment 3.
Fig. 5 is a schematic structural view of embodiment 4.
FIG. 6 is a schematic structural view of example 5.
FIG. 7 is a schematic structural view of example 7.
FIG. 8 is a schematic diagram of the structure of a cylindrical porous medium reactor.
Fig. 9 is a schematic structural view of embodiment 9.
FIG. 10 is a schematic structural view of example 10.
FIG. 11 is a schematic structural view of example 11.
Reference numerals:
101-a first air pipe, 1011-a high-temperature section of the air pipe, 102-a second air pipe, 103-a device shell and 104-a porous medium reactor;
201-upper hole, 202-outer wall of porous medium reactor, 203-inner wall of porous medium reactor, 204-porous medium, 205-central cavity, 206-lower hole;
3-a heat exchanger;
401-reactor upper cover plate, 402-reactor lower cover plate, 403-cover plate hole.
Detailed Description
The present invention will be described in further detail below.
Example 1
As shown in fig. 1 and fig. 2, a biogas autothermal reforming porous medium reactor includes a first gas pipe 101, a second gas pipe 102, a spherical device shell 103, and a spherical porous medium reactor 104. A gap is left between the device housing 103 and the porous medium reactor 104 to form a first space. The porous medium reactor 104 comprises a porous medium reactor outer wall 202, a porous medium reactor inner wall 203 and a porous medium 204 filled between the inner wall and the outer wall, wherein the porous medium 204 can be an inert porous medium, such as alumina, a catalyst, or a mixture of the catalyst and the inert porous medium. The porous media 204 may be of the same porosity or a mixture of porosities. The first gas pipe 101 is connected with the gas pipe high-temperature section 1011, and the gas pipe high-temperature section 1011 is positioned at the center of the porous medium reactor 104, so that the residence time of reaction gas in a high-temperature area can be prolonged, and complete reaction is facilitated.
In the porous medium 204, the reaction gas can form super adiabatic combustion, the combustion temperature is high, stable ignition is facilitated, and the reaction gas flows from outside to inside along the radius direction. The first space and the high-temperature reaction zone are communicated through the porous medium 204 to form a reaction gas inner passage, the flow cross-sectional area of the reaction gas inner passage is gradually changed, flame is favorably controlled in the porous medium 204, and meanwhile, in the central cavity 205 at the center of the spherical porous medium reactor 104, the high-temperature reaction zone is formed at the center of the central cavity 205 due to radiation heat release of the inner wall 203 of the porous medium reactor, so that the high-efficiency completion of the reaction is ensured. The first gas pipe 101 is inserted into the center of the central cavity 205 of the spherical porous medium reactor 104 from the upper hole 201 of the spherical porous medium reactor 104, so that the retention time of reaction gas in a high-temperature reaction zone can be prolonged, and complete reaction is facilitated. The second gas pipe 102 is inserted from above the first gas pipe 101 and passes through the lower hole 206 of the spherical porous medium reactor 104, so that the reaction gas can be heated by high-temperature gas, which is beneficial to ignition of the reaction gas, and meanwhile, the reaction temperature can be increased, which is beneficial to stable reaction.
The working process of the embodiment is as follows:
after entering the second gas pipe 102, the reaction gas mixture is preheated by the first gas pipe 101 and the high-temperature gas in the central cavity 205 in the center of the porous medium reactor 104, then passes through the first space between the device shell 103 and the spherical porous medium reactor 104, enters the porous medium reactor 104 from the outer wall 202 of the porous medium reactor 104 of the spherical porous medium reactor 104, generates an exothermic chemical reaction in the porous medium reactor 104, then enters the high-temperature reaction zone 205 in the center of the porous medium reactor 104, and is discharged out of the reaction device through the first gas pipe 101 after the chemical reaction is completed.
In this embodiment, the first air pipe 101 is an air outlet pipe, and the second air pipe 102 is an air inlet pipe.
Example 2
As shown in FIG. 3, the main difference from example 1 is that the device housing 103 and the porous medium reactor 104 are each in the shape of an ellipsoid.
Example 3
As shown in FIG. 4, the main difference from example 1 is that the apparatus housing 103 and the porous medium reactor 104 of the reaction apparatus are each in the shape of a spherical polyhedron.
Example 4
As shown in fig. 5, compared with embodiment 1, the main difference is that the second gas pipe 102 is wrapped around the outside of the first gas pipe 101 exposed to the device housing 103, and the reaction gas in the second gas pipe 102 is heated by the residual heat of the high-temperature gas in the first gas pipe 101. The second gas pipe 102 extends through the first space between the device housing 103 and the spherical porous medium reactor 104 and the upper side of the spherical porous medium reactor 104 into the central cavity 205 of the spherical porous medium reactor 104. The reaction gas enters the central cavity 205 of the spherical porous medium reactor 104 through the second gas pipe 102, flows from inside to outside along the radius of the spherical porous medium reactor 104, undergoes an autothermal reforming reaction in the spherical porous medium reactor 104, passes through the first space between the spherical porous medium reactor 104 and the device shell 103, and flows out of the reaction device through the first gas pipe 101.
Example 5
As shown in fig. 6, the main difference between this embodiment and embodiment 4 is that a heat exchanger 3 is provided between the second gas pipe 102 and the first gas pipe 101, and the heat of the high-temperature gas in the first gas pipe 101 is transferred to the reaction gas in the second gas pipe 102 through the heat exchanger 3.
Example 6
The main difference between this embodiment and embodiment 5 is that the flow direction of the reaction gas is opposite, i.e. the reaction gas enters the reaction device through the first gas pipe 101 and finally exits the reaction device through the second gas pipe 102. After entering the first gas pipe 101, the reaction gas passes through the heat exchanger 3, is heated by the high-temperature gas flowing out of the second gas pipe 102, then passes through the first space between the device shell 103 and the porous medium reactor 104, enters the porous medium reactor 104, undergoes an autothermal reforming reaction therein, and finally flows out of the reactor through the central cavity 205 and the second gas pipe 102.
Example 7
As shown in fig. 7 and 8, the main difference from example 1 is that the apparatus casing 103 and the porous medium reactor 104 are cylindrical in shape.
The cylindrical porous medium reactor 104 comprises a reactor upper cover plate 401, a porous medium reactor inner wall 203, a porous medium reactor outer wall 202 and a reactor lower cover plate 402. The second air tube 102 passes through a cover plate hole 403 in the upper cover plate. The space enclosed between the inner wall 203 of the porous medium reactor and the outer wall 202 of the porous medium reactor and the space enclosed between the upper cover plate 401 of the reactor and the lower cover plate 402 of the reactor is filled with the porous medium 204.
The second gas pipe 102 is connected with the high-temperature gas pipe section 1011, and the high-temperature gas pipe section 1011 is located at the center of the porous medium reactor 104, so that the retention time of reaction gas in the high-temperature region can be prolonged, and complete reaction is facilitated. The high temperature section 1011 of the gas pipe may have openings in the wall to facilitate the uniform distribution of the reactant gases within the porous media reactor 104.
The reaction gas can form super adiabatic combustion in the cylindrical porous medium reactor 104, the combustion temperature is high, stable ignition is facilitated, and meanwhile radiation heat release of the inner wall 203 of the peripheral porous medium reactor can form a high-temperature area in the center of the reaction device, so that stable reaction is guaranteed. The gradual change in gas flow cross-sectional area along the radius of the cylindrical porous media reactor 104 facilitates the control of the flame front within the porous media reactor 104.
The working process of the embodiment is as follows:
after entering the device through the first gas pipe 101, the reaction gas mixture is preheated by the high-temperature gas in the second gas pipe 102, then passes through the first space between the device shell 103 and the cylindrical porous medium reactor 104, enters the cylindrical porous medium reactor 104 from the outer wall 202 of the porous medium reactor of the cylindrical porous medium reactor 104 for chemical reaction, then enters the high-temperature reaction zone in the central cavity 205, and is discharged out of the reaction device through the high-temperature section 1011 of the gas pipe and the second gas pipe 102 after the autothermal reforming reaction is completed.
In this embodiment, the first air pipe 101 is an air inlet pipe, and the second air pipe 102 is an air outlet pipe.
Example 8
The main difference from example 7 is that the reaction gas flows in the opposite direction, i.e., after entering the reaction device from the second gas pipe 102, the reaction gas undergoes a chemical reaction and then flows out of the reaction device from the first gas pipe 101.
Example 9
As shown in fig. 9, the main difference compared with the embodiment 7 is that a heat exchanger 3 is added between a first gas pipe 101 and a second gas pipe 102 of the reaction device. The reaction gas is heated by the high-temperature gas in the second gas pipe 102 after entering the heat exchanger 3 from the first gas pipe 101, and then enters the reaction apparatus.
Example 10
As shown in fig. 10, the reaction gas enters the first space between the porous medium reactor 104 and the device housing 103 from the second gas pipe 102, enters the porous medium reactor 104 from the outer porous medium reactor wall 202 of the porous medium reactor 104, undergoes a chemical reaction therein, then flows out from the inner porous medium reactor wall 203 of the porous medium reactor 104, enters the high temperature reaction zone in the central cavity 205 of the reaction device, and then exits the reaction device through the first gas pipe 101 from the pores between the high temperature section 1011 of the gas pipe and the second gas pipe 102.
In this embodiment, the wall of the high temperature section 1011 of the gas pipe is perforated to ensure uniform distribution of the gas flow velocity in the porous media reactor 104. The high-temperature section 1011 of the gas return pipe extends into the middle of the porous medium reactor 104, which is beneficial to prolonging the reaction time of the high-temperature zone. The second air pipe 102 is inserted into the first air pipe 101 from the upper part of the first air pipe 101, passes through the air pipe high-temperature section 1011, passes through the lower baffle plate of the porous medium reactor 104, and then enters the first space between the porous medium reactor 104 and the device shell 103, so that the waste heat of the high-temperature gas can be fully utilized to heat the reaction gas, and the stable proceeding of the chemical reaction is facilitated.
Example 11
As shown in fig. 11, the main difference between this embodiment and embodiment 10 is that the apparatus housing 103, the porous medium reactor 104, the first gas pipe 101 and the second gas pipe 102 are all cylindrical polyhedrons.
The above embodiments are preferred embodiments of the present invention, but the present invention is not limited to the above embodiments, and any other changes, modifications, substitutions, combinations, and simplifications which do not depart from the spirit and principle of the present invention should be construed as equivalents thereof, and all such changes, modifications, substitutions, combinations, and simplifications are intended to be included in the scope of the present invention.
Claims (10)
1. A biogas autothermal reforming porous medium reaction device is characterized in that: the device comprises a device shell, a porous medium reactor arranged in the device shell, a first air pipe and a second air pipe which are respectively connected with the device shell;
a first space is arranged between the device shell and the porous medium reactor;
the center of the porous medium reactor is provided with a high-temperature reaction zone formed by focusing thermal radiation;
porous media are densely filled in the porous media reactor;
the first space is communicated with the high-temperature reaction zone through a porous medium to form a reaction gas inner passage;
the first air pipe, the reaction gas inner passage and the second air pipe are communicated in sequence.
2. The apparatus for autothermal reforming of biogas with porous media as recited in claim 1, wherein: the second air pipe is sleeved with the first air pipe.
3. The apparatus as claimed in claim 1, wherein the reaction apparatus comprises: the device shell is externally provided with a heat exchanger, and two ends of the heat exchanger are respectively connected to the first air pipe and the second air pipe.
4. The apparatus as claimed in claim 1, wherein the reaction apparatus comprises: the first air pipe sequentially penetrates through one side of the device shell and one side of the whole porous medium reactor and is connected to the first space, and the second air pipe sequentially penetrates through one side of the device shell and one side of the porous medium reactor and is connected to the high-temperature reaction area.
5. The apparatus as claimed in claim 1, wherein the reaction apparatus comprises: the first air pipe sequentially penetrates through one side of the device shell and one side of the porous medium reactor and is connected to the high-temperature reaction zone, and the second air pipe penetrates through one side of the device shell and is connected to the high-temperature reaction zone.
6. The apparatus as claimed in claim 1, wherein the reaction apparatus comprises: the first air pipe and the second air pipe are arranged on the upper side of the device shell.
7. The apparatus as claimed in claim 1, wherein the reaction apparatus comprises: in the porous medium in the reaction gas inner passage, the gas flow cross-sectional area gradually changes along the reaction gas flow path.
8. The apparatus as claimed in claim 1, wherein the reaction apparatus comprises: the porous medium reactor is spherical, ellipsoidal, spherical polyhedron, cylindrical or cylindrical polyhedron, and the shape of the casing of the device is matched with that of the porous medium reactor.
9. The apparatus for autothermal reforming of biogas with porous media as recited in claim 1, wherein: the porous medium is inert porous medium, catalyst or a mixture of the catalyst and the inert porous medium.
10. The apparatus as claimed in claim 1, wherein the reaction apparatus comprises: the porous medium has one or more porosities.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210282828.5A CN114804027A (en) | 2022-03-22 | 2022-03-22 | Reaction device for methane autothermal reforming porous medium |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210282828.5A CN114804027A (en) | 2022-03-22 | 2022-03-22 | Reaction device for methane autothermal reforming porous medium |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2622164A (en) * | 2022-05-26 | 2024-03-06 | Guangdong Brunp Recycling Technology Co Ltd | Modified iron phosphate precursor, modified lithium iron phosphate, and preparation methods therefor |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107539950A (en) * | 2017-09-29 | 2018-01-05 | 华南理工大学 | A kind of methane self-heating dry reforming reaction unit |
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- 2022-03-22 CN CN202210282828.5A patent/CN114804027A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107539950A (en) * | 2017-09-29 | 2018-01-05 | 华南理工大学 | A kind of methane self-heating dry reforming reaction unit |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2622164A (en) * | 2022-05-26 | 2024-03-06 | Guangdong Brunp Recycling Technology Co Ltd | Modified iron phosphate precursor, modified lithium iron phosphate, and preparation methods therefor |
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