CN104986729A - Preparation method for hydrogen and carbon dioxide through static bed - Google Patents
Preparation method for hydrogen and carbon dioxide through static bed Download PDFInfo
- Publication number
- CN104986729A CN104986729A CN201510363426.8A CN201510363426A CN104986729A CN 104986729 A CN104986729 A CN 104986729A CN 201510363426 A CN201510363426 A CN 201510363426A CN 104986729 A CN104986729 A CN 104986729A
- Authority
- CN
- China
- Prior art keywords
- level
- fixed
- bed reactor
- gas
- hydrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000001257 hydrogen Substances 0.000 title claims abstract description 41
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 41
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 36
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 title abstract description 6
- 239000001569 carbon dioxide Substances 0.000 title abstract description 4
- 238000002360 preparation method Methods 0.000 title abstract 5
- 230000003068 static effect Effects 0.000 title abstract 3
- 239000007789 gas Substances 0.000 claims abstract description 52
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000012159 carrier gas Substances 0.000 claims abstract description 16
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 5
- 238000000034 method Methods 0.000 claims description 28
- 235000011089 carbon dioxide Nutrition 0.000 claims description 12
- 238000010926 purge Methods 0.000 claims description 12
- 238000004519 manufacturing process Methods 0.000 claims description 9
- 239000000377 silicon dioxide Substances 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 238000000354 decomposition reaction Methods 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 5
- 238000011068 loading method Methods 0.000 claims description 5
- 238000012423 maintenance Methods 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 5
- 238000010792 warming Methods 0.000 claims description 5
- 239000006004 Quartz sand Substances 0.000 claims description 4
- 210000002268 wool Anatomy 0.000 claims description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 abstract 2
- 238000010408 sweeping Methods 0.000 abstract 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 239000010453 quartz Substances 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 29
- 238000005516 engineering process Methods 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000000746 purification Methods 0.000 description 4
- 230000007812 deficiency Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000000629 steam reforming Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Abstract
The invention relates to a preparation method for hydrogen and carbon dioxide through a static bed, and belongs to the technical field of energy preparation. The preparation method comprises the steps that firstly, pretreatment is conducted on Fe, FeO, Fe304 and Fe203; the pretreated Fe, FeO, Fe304 and Fe203 are filled through a feeding hopper in sequence and are uniformly distributed to a first-grade fixed bed reactor, a second-grade fixed bed reactor, a third-grade fixed bed reactor and a fourth-grade fixed bed reactor which are composed of quartz tubes or alundum tubes; sweeping gas is pumped into the fixed bed reactors, reducing gas CH4 or synthesis gas is pumped into the fist-grade fixed bed reactor to improve the temperature, and the CO2 is gathered; the sweeping gas is pumped, carrier gas and water vapor are pumped into the four grades of fixed bed reactors, and hydrogen is gathered at the outlet of the first-grade fixed bed reactor. According to the preparation method for hydrogen and carbon dioxide through the static bed, four grades of fixed beds are used as one unit, the CO2 is gathered in a purifying-reducing atmosphere, and the hydrogen is gathered through the water vapor at the same time.
Description
Technical field
The present invention relates to a kind of method that fixed bed prepares hydrogen and carbonic acid gas, belong to energy preparing technical field.
Background technology
The energy is the major issue that human kind sustainable development faces.Fossil energy, as the energy main now, be the important factor determining social development, but fossil energy burning can cause serious environment and ecology problem, such as " haze ", " Greenhouse effect " etc.These problems have enjoyed the concern of people, and " Copenhagen climate change conference " that be intended to discuss Global Green House Gas Emissions Reduction and low-carbon economy is subject to national governments and shows great attention to; National focus has been become especially at home from conservation culture since " 18 is large " and environment protection.
Along with the CO that the fossil energy fire rows such as rapid development of economy oil, Sweet natural gas are released
2amount is also in increase sharply.Therefore CO in minimizing combustion processes
2discharge, development CO
2trapping technique and find the just aobvious necessity very of clean energy, this is also the important channel alleviating Greenhouse effect.
Hydrogen Energy is the clean renewable resources of a kind of desirable low stain or no pollution.Countries in the world are dropped into the development & application of huge man power and material to Hydrogen Energy all in a large number and are studied.Along with the fast development of modern industry, Hydrogen Energy also becomes increasingly extensive in the application of every field, and its demand is also growing.Under the situation that particularly energy and environment problem is increasingly severe, the arrival promoting hydrogen economy has particularly important effect for Sustainable Socioeconomic Development.Cheap, the efficient hydrogen producing technology of exploitation can expand the source of hydrogen economy.Current, China major project in the works all using Hydrogen Energy as priority research areas, this has fully demonstrated the strategic position of Hydrogen Energy in energy development.
In current hydrogen producing technology, methane steam reforming (SMR) is considered to the method for most potentiality, natural gas steam reformation (CH
4+ H
2o → CO+3H
2), this process production technology is comparatively ripe, but energy consumption and production cost are all high, and facility investment is large, therefore study other hydrogen producing technology and equipment significant.The proposition of hydrogen production of chemical chain technology (CLH) can effectively improve above deficiency.CLH is derived from burning chemistry chains (CLC) technology, and its principle is shown below:
The first step: CH
4+ M
xo
y→ M
xo
y-δ+ CO
2+ 2H
2o
Second step: H
2o+ M
xo
y-δ→ M
xo
y+ H
2
With the burning chemistry chains oxygen carrier that iron-based oxide compound is chief active species, because of the performance of its excellence, be considered to a kind of oxygen carrier having very much industrial prospect.
At present, because reducing atmosphere complete oxidation cannot be H by single fixed-bed reactor
2o and CO
2, CO and the H that partial oxidation produces
2the waste of environmental pollution and resource can be caused.For above-mentioned deficiency, the present invention proposes to have employed multistage fixed bed reactor, to realize continuous, stable purification reducing atmosphere and hydrogen manufacturing.
Summary of the invention
For above-mentioned prior art Problems existing and deficiency, the invention provides a kind of method that fixed bed prepares hydrogen and carbonic acid gas.It is that a unit achieves purification reducing atmosphere trapping CO that the method utilizes with level Four fixed bed
2, trap hydrogen by water vapor, the present invention is achieved through the following technical solutions simultaneously.
A method for hydrogen and carbonic acid gas prepared by fixed bed, and its concrete steps are as follows:
(1) first by Fe, FeO, Fe
3o
4and Fe
2o
3dry 1 ~ 3h under temperature is 90 ~ 300 DEG C of conditions respectively, being then finely ground to granularity is 20 ~ 40 orders;
(2) Fe, FeO, the Fe that will process through step (1)
3o
4and Fe
2o
3successively with loading hopper filling and be distributed to uniformly the one-level of silica tube or alundum tube composition, secondary, three grades, in level Four fixed-bed reactor, separate with silica wool or quartz sand between each stage reactor two ends and bed;
(3) to the one-level of above-mentioned structure, secondary, three grades, pass into sweep gas in level Four fixed-bed reactor and purge 10 ~ 30min, purged in backward one-level fixed-bed reactor and passed into reducing gas CH
4or synthetic gas, with temperature rise rate be 5 ~ 10 DEG C/min by one-level, secondary, three grades, level Four fixed-bed reactor are warming up to 350 ~ 900 DEG C, by produce after reaction, from level Four fixed-bed reactor CO out
2trap, the H produced in the process
2o from level Four fixed-bed reactor out after condensation as the raw material of hydrogen production by water decomposition;
(4), after step (3) completes, stop passing into reducing gas CH
4or synthetic gas, pass into sweep gas and purge 10 ~ 30min, carrier gas and water vapour is passed in level Four fixed-bed reactor, by one-level, secondary, three grades, level Four fixed-bed reactor maintenance temperature to 200 ~ 750 DEG C, the dividing potential drop of water vapor is 25 ~ 60kPa, at one-level fixed-bed reactor outlet trapping hydrogen.
Fe, FeO, Fe in described step (2)
3o
4and Fe
2o
3add-on be respectively 5g ~ 20g.
Described step (3) and the middle sweep gas of step (4) are N
2, He or Ar, the flow that sweep gas passes into is 30 ~ 50ml/min.
Reducing gas CH in described step (3)
4or the flow that synthetic gas passes into is 50 ~ 100ml/min.
The flow that in described step (4), carrier gas and water vapour pass into is 50 ~ 100ml/min, and carrier gas is N
2, He or Ar.
The invention has the beneficial effects as follows: (1) multistage fixed bed application fully can realize the purification of reducing gas; (2) it is made to be converted into CO completely in purification reducing gas process
2and H
2o, decreasing pollution gas purging, simultaneously CO
2trapping can reduce the discharge of greenhouse gases.
Accompanying drawing explanation
Fig. 1 is the present invention is a unit trapping hydrogen and carbon dioxide process figure with level Four fixed bed.
Embodiment
Below in conjunction with the drawings and specific embodiments, the invention will be further described.
Embodiment 1
As shown in Figure 1, the method for hydrogen and carbonic acid gas prepared by this fixed bed, and its concrete steps are as follows:
(1) first by Fe, FeO, Fe
3o
4and Fe
2o
3dry 2h under temperature is 300 DEG C of conditions respectively, being then finely ground to granularity is 30 orders;
(2) Fe, FeO, Fe that 20g processes through step (1) is respectively got
3o
4and Fe
2o
3successively with loading hopper filling and be distributed to uniformly the one-level of silica tube composition, secondary, three grades, in level Four fixed-bed reactor, separate with silica wool between each stage reactor two ends and bed;
(3) to the one-level of above-mentioned structure, secondary, three grades, pass into sweep gas in level Four fixed-bed reactor and purge 30min, having purged in backward one-level fixed-bed reactor and having passed into flow is 100ml/min reducing gas CH
4, with temperature rise rate be 10 DEG C/min by one-level, secondary, three grades, level Four fixed-bed reactor are warming up to 900 DEG C, by produce after reaction, from level Four fixed-bed reactor CO out
2trap, the H produced in the process
2o from level Four fixed-bed reactor out after condensation as the raw material of hydrogen production by water decomposition; Wherein sweep gas is N
2, the flow that sweep gas passes into is 30ml/min;
(4), after step (3) completes, stop passing into reducing gas CH
4pass into sweep gas and purge 30min, carrier gas and water vapour is passed in level Four fixed-bed reactor, by one-level, secondary, three grades, level Four fixed-bed reactor maintenance temperature to 750 DEG C, the dividing potential drop of water vapor is 30kPa, at one-level fixed-bed reactor outlet trapping hydrogen, wherein sweep gas and carrier gas are N
2, the flow that sweep gas passes into is 30ml/min, and the flow that carrier gas and water vapour pass into is 100ml/min.
Embodiment 2
As shown in Figure 1, the method for hydrogen and carbonic acid gas prepared by this fixed bed, and its concrete steps are as follows:
(1) first by Fe, FeO, Fe
3o
4and Fe
2o
3dry 1h under temperature is 200 DEG C of conditions respectively, being then finely ground to granularity is 20 orders;
(2) Fe, FeO, Fe that 10g processes through step (1) is respectively got
3o
4and Fe
2o
3successively with loading hopper filling and be distributed to uniformly the one-level of alundum tube composition, secondary, three grades, in level Four fixed-bed reactor, separate with quartz sand between each stage reactor two ends and bed;
(3) to the one-level of above-mentioned structure, secondary, three grades, pass into sweep gas in level Four fixed-bed reactor and purge 20min, having purged in backward one-level fixed-bed reactor and having passed into flow is 80ml/min reducing gas CH
4, with temperature rise rate be 5 DEG C/min by one-level, secondary, three grades, level Four fixed-bed reactor are warming up to 400 DEG C, by produce after reaction, from level Four fixed-bed reactor CO out
2trap, the H produced in the process
2o from level Four fixed-bed reactor out after condensation as the raw material of hydrogen production by water decomposition; Wherein sweep gas is He, and the flow that sweep gas passes into is 50ml/min;
(4), after step (3) completes, stop passing into reducing gas CH
4pass into sweep gas and purge 20min, carrier gas and water vapour is passed in level Four fixed-bed reactor, by one-level, secondary, three grades, level Four fixed-bed reactor maintenance temperature to 500 DEG C, the dividing potential drop of water vapor is 60kPa, and at one-level fixed-bed reactor outlet trapping hydrogen, wherein sweep gas and carrier gas are He gas, the flow that sweep gas passes into is 50ml/min, and the flow that carrier gas and water vapour pass into is 80ml/min.
Embodiment 3
As shown in Figure 1, the method for hydrogen and carbonic acid gas prepared by this fixed bed, and its concrete steps are as follows:
(1) first by Fe, FeO, Fe
3o
4and Fe
2o
3dry 3h under temperature is 90 DEG C of conditions respectively, being then finely ground to granularity is 40 orders;
(2) Fe, FeO, Fe that 5g processes through step (1) is respectively got
3o
4and Fe
2o
3successively with loading hopper filling and be distributed to uniformly the one-level of alundum tube composition, secondary, three grades, in level Four fixed-bed reactor, separate with quartz sand between each stage reactor two ends and bed;
(3) to the one-level of above-mentioned structure, secondary, three grades, pass into sweep gas in level Four fixed-bed reactor and purge 10min, purging completes in backward one-level fixed-bed reactor and passes into flow is 50ml/min synthetic gas, with temperature rise rate be 8 DEG C/min by one-level, secondary, three grades, level Four fixed-bed reactor are warming up to 350 DEG C, by produce after reaction, from level Four fixed-bed reactor CO out
2trap, the H produced in the process
2o from level Four fixed-bed reactor out after condensation as the raw material of hydrogen production by water decomposition; Wherein sweep gas is Ar, and the flow that sweep gas passes into is 40ml/min;
(4) after step (3) completes, stop passing into synthetic gas, pass into sweep gas and purge 10min, in level Four fixed-bed reactor, pass into carrier gas and water vapour, by one-level, secondary, three grades, level Four fixed-bed reactor maintenance temperature to 200 DEG C, the dividing potential drop of water vapor is 25kPa, at one-level fixed-bed reactor outlet trapping hydrogen, wherein sweep gas and carrier gas are Ar, and the flow that sweep gas passes into is 40ml/min, and the flow that carrier gas and water vapour pass into is 50ml/min.
Below by reference to the accompanying drawings the specific embodiment of the present invention is explained in detail, but the present invention is not limited to above-mentioned embodiment, in the ken that those of ordinary skill in the art possess, various change can also be made under the prerequisite not departing from present inventive concept.
Claims (5)
1. a method for hydrogen and carbonic acid gas prepared by fixed bed, it is characterized in that concrete steps are as follows:
(1) first by Fe, FeO, Fe
3o
4and Fe
2o
3dry under temperature is 90 ~ 300 DEG C of conditions respectively, being then finely ground to granularity is 20 ~ 40 orders;
(2) Fe, FeO, the Fe that will process through step (1)
3o
4and Fe
2o
3successively with loading hopper filling and be distributed to uniformly the one-level of silica tube or alundum tube composition, secondary, three grades, in level Four fixed-bed reactor, separate with silica wool or quartz sand between each stage reactor two ends and bed;
(3) to the one-level of above-mentioned structure, secondary, three grades, pass into sweep gas in level Four fixed-bed reactor and purge 10 ~ 30min, purged in backward one-level fixed-bed reactor and passed into reducing gas CH
4or synthetic gas, with temperature rise rate be 5 ~ 10 DEG C/min by one-level, secondary, three grades, level Four fixed-bed reactor are warming up to 350 ~ 900 DEG C, by produce after reaction, from level Four fixed-bed reactor CO out
2trap, the H produced in the process
2o from level Four fixed-bed reactor out after condensation as the raw material of hydrogen production by water decomposition;
(4), after step (3) completes, stop passing into reducing gas CH
4or synthetic gas, pass into sweep gas and purge 10 ~ 30min, carrier gas and water vapour is passed in level Four fixed-bed reactor, by one-level, secondary, three grades, level Four fixed-bed reactor maintenance temperature to 200 ~ 750 DEG C, the dividing potential drop of water vapor is 25 ~ 60kPa, at one-level fixed-bed reactor outlet trapping hydrogen.
2. the method for hydrogen and carbonic acid gas prepared by fixed bed according to claim 1, it is characterized in that: Fe, FeO, Fe in described step (2)
3o
4and Fe
2o
3add-on be respectively 5g ~ 20g.
3. the method for hydrogen and carbonic acid gas prepared by fixed bed according to claim 1, it is characterized in that: described step (3) and the middle sweep gas of step (4) are N
2, He or Ar, the flow that sweep gas passes into is 30 ~ 50ml/min.
4. the method for hydrogen and carbonic acid gas prepared by fixed bed according to claim 1, it is characterized in that: reducing gas CH in described step (3)
4or the flow that synthetic gas passes into is 50 ~ 100ml/min.
5. the method for hydrogen and carbonic acid gas prepared by fixed bed according to claim 1, it is characterized in that: the flow that in described step (4), carrier gas and water vapour pass into is 50 ~ 100ml/min, and carrier gas is N
2, He or Ar.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510363426.8A CN104986729B (en) | 2015-06-29 | 2015-06-29 | Preparation method for hydrogen and carbon dioxide through static bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510363426.8A CN104986729B (en) | 2015-06-29 | 2015-06-29 | Preparation method for hydrogen and carbon dioxide through static bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104986729A true CN104986729A (en) | 2015-10-21 |
| CN104986729B CN104986729B (en) | 2017-05-10 |
Family
ID=54298659
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
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| CN (1) | CN104986729B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI572562B (en) * | 2016-05-26 | 2017-03-01 | 行政院原子能委員會核能研究所 | Reactor of Hydrocarbon Fuel Having Space Efficiency for Separating and Purifying Carbon Dioxide |
Citations (4)
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|---|---|---|---|---|
| US4435379A (en) * | 1982-08-18 | 1984-03-06 | The Dow Chemical Company | Process for treating chlorinated hydrocarbons |
| EP0431819A1 (en) * | 1989-11-28 | 1991-06-12 | Yutaka Tamaura | Method for decomposing gaseous oxide and catalyst used therefor |
| CN101164864A (en) * | 2007-09-28 | 2008-04-23 | 昆明理工大学 | Catalytic methane cracking hydrogen production and two-step method making synthesized gas method |
| CN101177241A (en) * | 2007-11-05 | 2008-05-14 | 昆明理工大学 | Method for preparing synthesis gas by the catforming of methyl hydride and carbonic anhydride in molten salt |
-
2015
- 2015-06-29 CN CN201510363426.8A patent/CN104986729B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4435379A (en) * | 1982-08-18 | 1984-03-06 | The Dow Chemical Company | Process for treating chlorinated hydrocarbons |
| EP0431819A1 (en) * | 1989-11-28 | 1991-06-12 | Yutaka Tamaura | Method for decomposing gaseous oxide and catalyst used therefor |
| CN101164864A (en) * | 2007-09-28 | 2008-04-23 | 昆明理工大学 | Catalytic methane cracking hydrogen production and two-step method making synthesized gas method |
| CN101177241A (en) * | 2007-11-05 | 2008-05-14 | 昆明理工大学 | Method for preparing synthesis gas by the catforming of methyl hydride and carbonic anhydride in molten salt |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI572562B (en) * | 2016-05-26 | 2017-03-01 | 行政院原子能委員會核能研究所 | Reactor of Hydrocarbon Fuel Having Space Efficiency for Separating and Purifying Carbon Dioxide |
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|---|---|
| CN104986729B (en) | 2017-05-10 |
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