CN105776133A - Methane reforming system - Google Patents
Methane reforming system Download PDFInfo
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- CN105776133A CN105776133A CN201610112216.6A CN201610112216A CN105776133A CN 105776133 A CN105776133 A CN 105776133A CN 201610112216 A CN201610112216 A CN 201610112216A CN 105776133 A CN105776133 A CN 105776133A
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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
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
- C01B3/26—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons 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
- 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
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
The invention provides a methane reforming system.In the system, a methane and vapor pipeline passes through a hydrogen separation device and a carbon dioxide separation device in sequence in a circulating mode, hydrogen and carbon dioxide generated from wet reformation of methane are separated alternately to promote methane reformation reaction equilibrium to move to the forward direction, and then methane conversion rate is increased greatly compared with a one-time reaction conversion rate under the non-circulating condition.Besides, a heat exchanger is additionally arranged between the hydrogen separation device and the carbon dioxide device to recover lost heat generated by difference in operation temperatures of the hydrogen separation device and the carbon dioxide separation device, so that the energy utilization rate of the system is increased.
Description
Technical field
The present invention relates to new forms of energy (regenerative resource) technical field, particularly relate to a kind of methane reformer system.
Background technology
Hydrogen is the clean energy resource that a kind of energy density is significantly high, and how high efficiency, low cost ground hydrogen making is the focus that current various countries are studied.Industrial hydrogen production mode traditional at present is mainly through methane and steam reforming, reaction temperature is more than 700 DEG C, not only the heat resistance of equipment is required higher, and methane reforming reaction needs to absorb amount of heat, these energy mostly come from fossil energy burning, energy expenditure is relatively big, and the energy utilization efficiency of methane reformer system is relatively low.
Summary of the invention
(1) to solve the technical problem that
The invention provides a kind of methane reformer system, to reduce methane reforming hydrogen making cost, improve methane conversion.
(2) technical scheme
Methane reformer system of the present invention includes: hydrogen separation device, and its medial compartment is divided into first kind region and Equations of The Second Kind region, wherein, and the hydrogen dividing potential drop in Equations of The Second Kind region when the hydrogen dividing potential drop in first kind region is less than methane and steam reforming reaction；Carbon dioxide separation device, its medial compartment is divided into the 3rd class region and the 4th class region, wherein, the partial pressure of carbon dioxide in the 3rd class region is less than the partial pressure of carbon dioxide in the 4th class region when methane and steam reforming reaction, and, the import in the 4th class region is connected to the outlet in Equations of The Second Kind region, and the outlet in the 4th class region is connected to the import in Equations of The Second Kind region.Wherein, methane and steam enter the Equations of The Second Kind region of hydrogen separation device, and methane reforming reaction occurs, and the hydrogen of generation enters first kind region, and reforming reaction balance moves to forward, and unreacting gas continues reaction；Then, in Equations of The Second Kind region, reacted gas enters the 4th class region of carbon dioxide separation device, and after separating hydrogen gas, remaining carbon dioxide enters the 3rd class region；Then, the residual gas in the 4th class region reenters the Equations of The Second Kind region of hydrogen separation device and carries out methane reforming reaction.
(3) beneficial effect
From technique scheme it can be seen that methane reformer system of the present invention has the advantages that
(1) methane and steam pipeline flow through hydrogen separation device and carbon dioxide separation device successively and form circulation, methane wet reformate hydrogen and carbon dioxide are alternately separated, promote methane reforming reaction balance to move to forward, make methane conversion significantly promote compared to single reaction conversion ratio；
(2) between hydrogen separation device and carbon dioxide separation device, increase heat exchanger, reclaim because hydrogen separation device caused thermal losses different from the operation temperature of carbon dioxide separation device, enable the system to utilization rate and promote；
(3) hydrogen separation device can adopt membrane material to separate with carbon dioxide separation device, membrane material segregation apparatus adopts barrel forms, many membrane material pipelines can be placed in chamber outer wall 5, be conducive to increasing membrane material specific surface area, improve space availability ratio；
(4) system can combine with discarded energy such as the new forms of energy such as solar energy or nuclear energy and industrial waste heats, clean environment firendly.
Accompanying drawing explanation
Fig. 1 is the structural representation of methane reformer system according to a first embodiment of the present invention；
Fig. 2 is membrane material segregation apparatus schematic diagram in methane reformer system shown in Fig. 1；
Fig. 3 is front 4 the circulation methane remaining proportions in hydrogen separation device and carbon dioxide separation device at 400 DEG C of methane reformer system shown in Fig. 1；
Fig. 4 is front 4 the recirculated water steams remaining proportion in hydrogen separation device and carbon dioxide separation device at 400 DEG C of methane reformer system shown in Fig. 1.
[main element of the present invention meets explanation]
1-hydrogen separation device；2-heat exchanger；
3-carbon dioxide separation device；4-solar-energy light collector；
5-chamber outer wall；6-membrane material pipeline；
7-reaction gas inlet；8-product separated region.
Detailed description of the invention
The present invention utilizes catalyst methane reforming, and alternately separates product, and the mode circulated by unreacting gas can make reaction temperature significantly reduce to less than 400 DEG C, if disregarding methane oxidizing archaea, methane conversion is up to 100%.
For making the object, technical solutions and advantages of the present invention clearly understand, below in conjunction with specific embodiment, and with reference to accompanying drawing, the present invention is described in more detail.
One, first embodiment
In one exemplary embodiment of the present invention, it is provided that a kind of methane reformer system.Fig. 1 is the structural representation of methane reformer system according to a first embodiment of the present invention.As it is shown in figure 1, the present embodiment one methane reformer system includes: hydrogen separation device 1；Heat exchanger 2；Carbon dioxide separation device 3；And solar-energy light collector 4.Wherein, hydrogen separation device 1 and carbon dioxide separation device 3 all adopt membrane material segregation apparatus.
Refer to Fig. 1, the medial compartment of hydrogen separation device 1 is divided into the first kind region of two class regions-hydrogen permeation membrane separation side and the Equations of The Second Kind region of hydrogen permeation membrane unstripped gas supply side by hydrogen permeation membrane.Wherein, the hydrogen dividing potential drop in first kind region is less than the hydrogen dividing potential drop in Equations of The Second Kind region when methane and steam reforming reaction.
Refer to Fig. 1, the medial compartment of carbon dioxide separation device 3 is divided into the 3rd class region of two class regions-saturating carbon dioxide membrane separation side and the 4th class region of saturating carbon dioxide membrane unstripped gas supply side by saturating carbon dioxide membrane.Wherein, the partial pressure of carbon dioxide in saturating 4th class region when the partial pressure of carbon dioxide in the 3rd class region is less than methane and steam reforming.
Fig. 2 is membrane material segregation apparatus schematic diagram in methane reformer system shown in Fig. 1.Refer to Fig. 2, membrane material segregation apparatus adopts barrel forms.Many membrane material pipelines are placed in chamber outer wall 5.This membrane material pipeline is prepared by corresponding membrane material, for instance:
(1) in hydrogen separation device 1, membrane material pipeline is prepared by hydrogen permeating material, is internally formed Equations of The Second Kind region at membrane material pipeline, forms first kind region between membrane material pipeline and chamber outer wall.First area can connect vacuum pump or pass into noble gas or hydrogen partial pressure drops in oxidizing gas；
(2) in carbon dioxide separation device 3, membrane material pipeline by saturating carbon dioxide film preparation, is internally formed the 4th class region at membrane material pipeline, forms the 3rd class region between membrane material pipeline and chamber outer wall.3rd class region can connect vacuum pump or pass into noble gas or reducibility gas reduction partial pressure of carbon dioxide.
In this membrane material segregation apparatus, reacting gas is entered by reaction gas inlet 7, carries out methane reforming reaction at membrane material pipeline, generates the product separated region 8 outside gas traverse membrane material pipeline.
In whole methane reformer system, methane and steam enter the Equations of The Second Kind region of hydrogen separation device 1, and reforming reaction occurs, and the hydrogen of generation enters first kind region, and reforming reaction balance moves to forward, and unreacting gas continues reaction；Then, in Equations of The Second Kind region, reacted gas enters the 4th class region of carbon dioxide separation device 3, and after separating hydrogen gas, remaining carbon dioxide enters the 3rd class region；Then, the residual gas in the 4th class region reenters the Equations of The Second Kind region of hydrogen separation device 1.
In the present embodiment, methane and steam pipeline flow through hydrogen separation device and carbon dioxide separation device successively and form circulation, methane wet reformate hydrogen and carbon dioxide are alternately separated, promote methane reforming reaction balance to move to forward, make methane conversion significantly promote compared to single reaction conversion ratio.
Wherein, hydrogen separation device 1 and carbon dioxide separation device 3 all can as the reaction chambers of methane and steam reforming.The operating temperature of hydrogen separation device 1 is greater than the occurrence temperature of methane and steam reforming reaction, is generally greater than 400 DEG C, but can reduce reaction temperature to more than 100 DEG C by applying the mode of potential difference or ionization reaction thing at methane and steam reforming region.
In the present embodiment, hydrogen separation device and carbon dioxide separation device operation temperature can differ, for instance when hydrogen separation device is palladium film, saturating hydrogen temperature is typically in more than 400 DEG C；When carbon dioxide separation device is organic carbon dioxide separation film, carbon dioxide separation temperature is generally room temperature, and the heat exchanger 2 that now can pass through to connect in the middle of pipeline carries out heat recovery.
Refer to Fig. 1, for heat exchanger 2: its heater gas inlet port is connected to the gas outlet in the Equations of The Second Kind region of hydrogen separation device 1, its hot gas outlet is connected to the gas feed in the 4th class region of carbon dioxide separation device 3；Its cold air entrance is connected to the gas outlet in the 4th class region of carbon dioxide separation device 3, and the outlet of its cold air is connected to the gas feed in the Equations of The Second Kind region of hydrogen separation device 1.
In the present embodiment, by increasing heat exchanger, it is possible to reclaim because hydrogen separation device caused thermal losses different from the operation temperature of carbon dioxide separation device, enable the system to utilization rate and promote.
Although it should be noted that adopt hydrogen permeation membrane and saturating carbon dioxide membrane to come hydrogen and the carbon dioxide of the whole generation of methane weight in wet base in piece-rate system in the present embodiment, but the present invention is not limited thereto.For example:
(1) for hydrogen separation device 1, the mode of separating hydrogen gas can also add absorption hydrogen material in the medial compartment of hydrogen separation device 1, such as activated carbon and oxide, now, the hydrogen dividing potential drop adding the region absorbing hydrogen material is less than not adding the hydrogen dividing potential drop in the region absorbing hydrogen material；
(2) for carbon dioxide separation device 3, the mode reducing partial pressure of carbon dioxide is not limited in the present embodiment to utilize organic carbon dioxide membrane or the mode of inorganic carbon dioxide membrane, absorbing carbon dioxide material can also be added, for instance alkaline solution, basic anhydride, activated carbon in carbon dioxide separation device 3.Now, the hydrogen dividing potential drop in the region adding absorbing carbon dioxide material is less than not adding the partial pressure of carbon dioxide in the region of absorbing carbon dioxide material.
Those skilled in the art it should be understood that, in above-mentioned two situations, the change of corresponding dividing potential drop is continually varying, and the division of this time domain is also that two class regions in two chambers are not separated by real rete in virtual sense.
In the present embodiment, groove type solar condenser is by solar light focusing in the Equations of The Second Kind region of hydrogen separation device 1, and needed for converting the solar into heat energy confession reforming reaction therein, but the present invention is not limited thereto.For example:
(1) for solar-energy light collector, it is also possible to adopt Fresnel solar concentrator, disc type solar energy condenser, or tower type solar condenser converts solar energy into heat energy；
(2) for energy source, this device can be provided energy by solar energy, heat can also be provided by nuclear energy, fossil energy or industrial waste heat, energy is provided by solar energy or nuclear energy, can reducing the use of electric energy and fossil energy, the sustainable development for realizing the energy is significant.
During the present embodiment methane reformer system adopts, low-temperature solar energy is energy source, and reaction temperature controls more than 400 DEG C.But the present invention is not limited thereto.Further, when the whole conversion zone applying electric field of methane weight in wet base is reduced methane reforming temperature by utilization, operating temperature just can complete the present invention more than 100 DEG C.
The material of hydrogen permeation membrane and saturating carbon dioxide membrane is all well known to those skilled in the art, only provides several conventional material herein, by way of example, hydrogen permeation membrane material is selected from the one in following material: ZrO2-TiO2-Y2O3；SrCexTm1-xO3-δ(0≤x≤1,0≤δ < 3)；SrCexYb1-xO3-α(0≤x≤1,0≤α < 3) and palladium (Pd).Saturating carbon dioxide membrane material is selected from the one in following material: the La of doping fused carbonate (moltencarbonate, lower same)1-xSrxCo1-yFeyO3-δ(0≤x≤1,0≤δ < 3)；Doping Y2O3ZrO with fused carbonate2；Doping Gd2O3CeO with fused carbonate2。
Although it should be noted that hydrogen is the main purpose of the present embodiment, but carbon dioxide is also useful.Carbon dioxide being in great demand in medical treatment, chemical industry, oil exploration & development etc..
Additionally, due to inorganic film reactor only allows a kind of gas permeation, the hydrogen therefore produced and carbon dioxide purity are all very high.Regardless of whether be high-purity hydrogen or high-purity carbon dioxide, it is worth all significantly high.Current industrial high-volume hydrogen making reacts essentially from gas renormalizing, and in product, the carbon monoxide of residual is not easily removed completely；Industrial mass is produced carbon dioxide and is mainly carried out limestone calcination, and energy consumption is relatively big, and energy utilization efficiency is not high.Utilize the present embodiment methane reformer system Production of High-purity Hydrogen, high-purity carbon dioxide can seldom contain other impurity, settle at one go, significant in energy source and power, medical treatment, chemical industry, oil exploration etc., there is good application value.
In the present embodiment, whole system with focus on solar energy for energy source, control device internal temperature be 400 DEG C.When methane and the steam inflow hydrogen separation device 1 of preheating, the hydrogen that methane and steam reforming produce can be separated system, promotes the whole continuation of methane weight in wet base carry out to forward and produce more product.When hydrogen partial pressure declines, after partial pressure of carbon dioxide rises, hydrogen permeation membrane both sides hydrogen partial pressure difference is gradually lowered, and partial pressure of carbon dioxide raises, and hinders reaction to carry out to forward further.Mixing gas inflow heat exchanger 2 in hydrogen separation device 1 carries out heat recovery, and continue to flow into carbon dioxide separation device 3, owing in now gaseous mixture body, partial pressure of carbon dioxide is higher, carbon dioxide separation can be gone out system through saturating carbon dioxide membrane, promote methane and steam to reform further and produce more hydrogen and carbon dioxide.Along with hydrogen partial pressure raises, partial pressure of carbon dioxide reduces, methane and steam reforming reaction speed progressively slow down, and are not now separated the admixture of gas of system and again flow into hydrogen separation device 1 and repeat said process until methane and steam are fully converted to hydrogen and carbon dioxide and are separated system.Hydrogen and carbon dioxide are collected separately.
Fig. 3 is front 4 the circulation methane remaining proportions in hydrogen separation device and carbon dioxide separation device at 400 DEG C of methane reformer system shown in Fig. 1.Wherein 1,2,3,4 being illustrated respectively in four circulations methane remaining proportion in hydrogen permeation membrane, 1 ', 2 ', 3 ', 4 ' are illustrated respectively in methane remaining proportion in four circulation carbon dioxide separation devices；
Fig. 4 is front 4 the recirculated water steams remaining proportion in hydrogen separation device and carbon dioxide separation device at 400 DEG C of methane reformer system shown in Fig. 1.Wherein 1,2,3,4 being illustrated respectively in four circulations steam remaining proportion in hydrogen permeation membrane, 1 ', 2 ', 3 ', 4 ' are illustrated respectively in steam remaining proportion in four circulation carbon dioxide separation devices；
By Fig. 3, Fig. 4, by circulating unreacting gas, it is possible to make methane and steam transforming rate be greatly improved, and namely 3 later conversion ratios of circulation are increased to more than 99%, and the methane conversion of tradition methane reforming method only has about 15% when 400 DEG C, this method has a clear superiority in by contrast.
Through calculating, methane and steam are after 5 hydrogen separation devices and carbon dioxide separation device, and methane and the steam resolution ratio of this system all reach more than 99.9%.
Two, the second embodiment
In second exemplary embodiment of the present invention, additionally provide another low temperature methane reformer system.This system and first embodiment are different in that, by applying potential difference at methane and steam reforming reaction region so that reaction temperature dramatic drop-off is near 100 DEG C.Generally, potential difference absolute value delta V meets: 0V < Δ V≤1000V.
It should be noted that except adopting and applying potential difference reduction reaction temperature, it is also possible to adopt the mode of ionization reaction thing to reduce reaction temperature, no longer enumerate one by one herein.
So far, already in connection with accompanying drawing, two embodiments of the present invention have been described in detail.According to above description, methane reformer system of the present invention should have been had and clearly recognized by those skilled in the art.
It should be noted that in accompanying drawing or description text, the implementation not illustrating or describing, it is in art form known to a person of ordinary skill in the art, is not described in detail.Additionally, the above-mentioned definition to each element and method is not limited in various concrete structures, shape or the mode mentioned in embodiment, it can be carried out change simply or replace by those of ordinary skill in the art, for instance:
(1) except passing through arrange hydrogen permeation membrane in hydrogen separation device or absorb hydrogen material, it is also possible to adopt other modes to make the hydrogen dividing potential drop hydrogen dividing potential drop less than the Equations of The Second Kind region of another part in first kind region therein；
(2) except passing through to center carbon dioxide membrane or absorbing carbon dioxide material at carbon dioxide separation dress, it is also possible to adopt other modes to make the partial pressure of carbon dioxide partial pressure of carbon dioxide less than the 4th class region of another part in the 3rd class region therein；
(3) about absorb hydrogen material, absorbing carbon dioxide material, hydrogen permeation membrane material, saturating carbon dioxide material, its be not limited in above-described embodiment provide all kinds of concrete material；
(4) demonstration of the parameter comprising particular value can be provided herein, but these parameters are without being definitely worth equal to corresponding, but analog value can be similar in acceptable error margin or design constraint；
(5) the direction term mentioned in embodiment, for instance " on ", D score, "front", "rear", "left", "right" etc., be only the direction with reference to accompanying drawing, be not used for limiting the scope of the invention；
(6) above-described embodiment can based on the consideration of design and reliability, and the collocation that is mixed with each other uses or uses with other embodiment mix and match, and namely the technical characteristic in different embodiments can freely form more embodiment.
In sum, in methane reformer system of the present invention, pipeline is sequentially connected with hydrogen separation device, heat exchanger, carbon dioxide separation device and connects back to hydrogen separation device again, make unstripped gas can flow through hydrogen separation device, heat exchanger, carbon dioxide separation device successively, and non-separation gas body weight is newly flowed back to hydrogen separation device be circulated.When solving by single hydrogen permeation membrane, due to the problem that the too high suppression methane reforming reaction forward of partial pressure of carbon dioxide moves, and improve methane reforming reaction conversion ratio by circular response, the thermal losses caused because of the front and back device temperature difference is reclaimed by heat exchanger, it is that system capacity utilization rate promotes, there is stronger practical value.
Particular embodiments described above; the purpose of the present invention, technical scheme and beneficial effect have been further described; it is it should be understood that; the foregoing is only specific embodiments of the invention; it is not limited to the present invention; all within the spirit and principles in the present invention, any amendment of making, equivalent replacement, improvement etc., should be included within protection scope of the present invention.
Claims (10)
1. a methane reformer system, it is characterised in that including:
Hydrogen separation device (1), its medial compartment is divided into first kind region and Equations of The Second Kind region, wherein, the hydrogen dividing potential drop in Equations of The Second Kind region when the hydrogen dividing potential drop in first kind region is less than methane and steam reforming reaction；
Carbon dioxide separation device (3), its medial compartment is divided into the 3rd class region and the 4th class region, wherein, the partial pressure of carbon dioxide in the 3rd class region is less than the partial pressure of carbon dioxide in the 4th class region when methane and steam reforming reaction, and, the import in the 4th class region is connected to the outlet in Equations of The Second Kind region, and the outlet in the 4th class region is connected to the import in Equations of The Second Kind region
Wherein, methane and steam enter the Equations of The Second Kind region of hydrogen separation device (1), and methane reforming reaction occurs, and the hydrogen of generation enters first kind region, and reforming reaction balance moves to forward, and unreacting gas continues reaction；Then, in Equations of The Second Kind region, reacted gas enters the 4th class region of carbon dioxide separation device (3), and after separating hydrogen gas, remaining carbon dioxide enters the 3rd class region；Then, the residual gas in the 4th class region reenters the Equations of The Second Kind region of hydrogen separation device (1) and carries out methane reforming reaction.
2. methane reformer system according to claim 1, it is characterised in that:
Described first kind region adds absorption hydrogen material, or connects vacuum pump, or passes into noble gas or oxidizing gas, so that the hydrogen dividing potential drop in Equations of The Second Kind region when the hydrogen dividing potential drop in this first kind region is less than methane and steam reforming reaction；And/or
Described 3rd class region adds absorbing carbon dioxide material, or connects vacuum pump, or passes into noble gas or reducibility gas, so that the partial pressure of carbon dioxide in the 4th class region when the partial pressure of carbon dioxide in the 3rd class region is less than methane and steam reforming reaction.
3. methane reformer system according to claim 1, it is characterised in that:
The medial compartment of described hydrogen separation device (1) is divided into two class regions by hydrogen permeation membrane, and wherein, described first kind region is the class region of hydrogen permeation membrane separation side；Described Equations of The Second Kind region is the class region of hydrogen permeation membrane unstripped gas supply side；
The medial compartment of described carbon dioxide separation device (3) is divided into two class regions by saturating carbon dioxide membrane, wherein, described 3rd class region is the class region of carbon dioxide membrane separation side, and described 4th class region is the class region of carbon dioxide membrane unstripped gas supply side.
4. methane reformer system according to claim 1, it is characterised in that also include: heat exchanger (2), for this heat exchanger (2):
Its heater gas inlet port is connected to the gas outlet in Equations of The Second Kind region, and its hot gas outlet is connected to the gas feed in the 4th class region；
Its cold air entrance is connected to the gas outlet in the 4th class region, and the outlet of its cold air is connected to the gas feed in Equations of The Second Kind region.
5. methane reformer system according to claim 1, it is characterised in that also include:
Heat provides device, is used for providing heat for needed for the reforming reaction in described hydrogen separation device (1), and its heat is provided by solar energy, nuclear energy, fossil energy or industrial waste heat.
6. methane reformer system according to claim 5, it is characterised in that described energy production arrangement is solar-energy light collector (4)；
Solar light focusing in the hydrogen permeation membrane unstripped gas supply side of hydrogen separation device (1), is converted the solar into heat energy for needed for reforming reaction therein by this solar-energy light collector (4).
7. methane reformer system according to claim 6, it is characterized in that, described solar-energy light collector (4) is one or more following combination: groove type solar condenser, tower type solar condenser, disc type solar energy condenser and Fresnel solar concentrator.
8. methane reformer system according to claim 1, it is characterised in that the Equations of The Second Kind region in described hydrogen separation device (1) and/or the 4th class region in described carbon dioxide separation device (3) are as reforming reaction region；
Wherein, each class region comprises at least one region, adopts the mode applying potential difference or ionization reaction thing to reduce reaction temperature in reforming reaction region.
9. methane reformer system according to any one of claim 1 to 8, it is characterised in that described hydrogen permeation membrane material is selected from the one in following material:
ZrO2-TiO2-Y2O3；
SrCexTm1-xO3-δ, wherein 0≤x≤1,0≤δ < 3；
SrCexYb1-xO3-α, wherein 0≤x≤1,0≤α < 3；With
Pd。
10. methane reformer system according to any one of claim 1 to 8, it is characterised in that described carbon dioxide membrane material is selected from the one in following material:
The La of doping fused carbonate1-xSrxCo1-yFeyO3-δ, wherein 0≤x≤1,0≤δ < 3；
Doping Y2O3ZrO with fused carbonate2；
Doping Gd2O3CeO with doping fused carbonate2。
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| CN107930552A (en) * | 2017-11-20 | 2018-04-20 | 武汉大学 | Solar energy hydrogen permeation membrane reaction unit and application method |
| CN110483228A (en) * | 2018-11-06 | 2019-11-22 | 中国科学院青岛生物能源与过程研究所 | A kind of method and apparatus reacted in proton-conductive films reactor while obtaining high-purity hydrogen and chemicals |
| CN112512681A (en) * | 2018-06-21 | 2021-03-16 | 巴泰勒纪念研究所 | Enhanced microchannel or mesochannel device and additive manufacturing method thereof |
| CN114314510A (en) * | 2022-01-29 | 2022-04-12 | 中国科学院工程热物理研究所 | Methane reforming reaction system |
| US11322766B2 (en) | 2020-05-28 | 2022-05-03 | Saudi Arabian Oil Company | Direct hydrocarbon metal supported solid oxide fuel cell |
| CN114988360A (en) * | 2022-05-13 | 2022-09-02 | 中国成达工程有限公司 | Method for preparing synthesis gas by natural gas partial oxidation and carbon dioxide self-heating reforming |
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| US11492255B2 (en) | 2020-04-03 | 2022-11-08 | Saudi Arabian Oil Company | Steam methane reforming with steam regeneration |
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| WO2023142929A1 (en) * | 2022-01-29 | 2023-08-03 | 中国科学院工程热物理研究所 | Methane reforming reaction system |
| CN114314510B (en) * | 2022-01-29 | 2023-11-03 | 中国科学院工程热物理研究所 | Methane reforming reaction system |
| CN114314510A (en) * | 2022-01-29 | 2022-04-12 | 中国科学院工程热物理研究所 | Methane reforming reaction system |
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