CN111422830A - Sewage treatment plant biogas hydrogen production system and method - Google Patents
Sewage treatment plant biogas hydrogen production system and method Download PDFInfo
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 239000001257 hydrogen Substances 0.000 title claims abstract description 56
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 56
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 27
- 239000010865 sewage Substances 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 15
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 52
- 230000003647 oxidation Effects 0.000 claims abstract description 48
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000001301 oxygen Substances 0.000 claims abstract description 47
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 47
- 238000000855 fermentation Methods 0.000 claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 12
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 8
- 230000023556 desulfurization Effects 0.000 claims abstract description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 6
- 238000006722 reduction reaction Methods 0.000 claims description 47
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 43
- 239000007789 gas Substances 0.000 claims description 31
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 230000015572 biosynthetic process Effects 0.000 claims description 11
- 238000003786 synthesis reaction Methods 0.000 claims description 11
- 238000001354 calcination Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 239000010802 sludge Substances 0.000 claims description 9
- 239000002250 absorbent Substances 0.000 claims description 8
- 230000002745 absorbent Effects 0.000 claims description 7
- 239000000969 carrier Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 18
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 7
- 238000000629 steam reforming Methods 0.000 description 7
- 230000008878 coupling Effects 0.000 description 4
- 238000010168 coupling process Methods 0.000 description 4
- 238000005859 coupling reaction Methods 0.000 description 4
- SZVJSHCCFOBDDC-UHFFFAOYSA-N ferrosoferric oxide Chemical compound O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 235000011089 carbon dioxide Nutrition 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000001133 acceleration Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
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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
-
- 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
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/10—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with metals
- C01B3/105—Cyclic methods
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention discloses a sewage treatment plant biogas hydrogen production system and a method, wherein a biogas outlet of an anaerobic fermentation tank is communicated with an inlet of a reduction reactor through a desulfurization adsorption device and a nitrogen and oxygen removal device, an outlet of the reduction reactor is communicated with an inlet of a first separator, a solid outlet of the first separator is communicated with an inlet of an oxidation reactor, an outlet of the oxidation reactor is communicated with an inlet of a second separator, a solid outlet of the second separator is communicated with an inlet of a calciner, an outlet of the calciner is communicated with an inlet of a third separator, a solid outlet of the third separator is communicated with an inlet of the reduction reactor, and an outlet of a steam pipeline is communicated with an inlet of the reduction reactor and an inlet of the oxidation reactor.
Description
Technical Field
The invention belongs to the field of environmental protection and hydrogen energy, and relates to a system and a method for producing hydrogen by using marsh gas from a sewage treatment plant.
Background
With the acceleration of the urbanization process in China, the discharge amount of sewage and the scale of sewage treatment plants are increased continuously. By 2020, the sewage treatment capacity is expected to reach 2.86 million cubic meters per hour, the activated sludge method is a common sewage treatment mode in China, and the annual output of associated sludge can also reach 26.8 million tons. In recent years, the state has vigorously advocated anaerobic fermentation to treat sludge, realize reduction, harmlessness and stabilization of sludge, and simultaneously generate clean energy, namely methane. At present, the sewage treatment plant usually uses the methane generated by anaerobic fermentation of sludge as energy gas to generate heat and generate power, the utilization mode is too simple, and the full recycling of the methane is difficult to realize. Therefore, a novel efficient methane utilization means is sought, and the method has important significance for improving economic and environmental benefits of sewage treatment plants.
In recent years, hydrogen fuel cell technology has been rapidly developed, and the proportion of hydrogen energy in future energy systems is increased. As a power source material for fuel cells, high-purity hydrogen gas will meet a large market demand. Therefore, the method for preparing high-purity hydrogen by adopting the marsh gas of the sewage treatment plant is a conversion path with wide prospect. The main component of the methane is methane, and the hydrogen production process by methane steam reforming is mature and is a main mode for producing hydrogen on a large scale. However, the steam reforming product needs to be subjected to subsequent treatment processes such as steam shift, pressure swing adsorption and the like to obtain high-purity hydrogen, and the problem of large carbon dioxide emission exists if the carbon capture technology is not combined. Researchers at home and abroad put forward various methods to improve the methane hydrogen production technology. The core of the adsorption-enhanced reforming technology is that CO is added in the reforming process of the carbon-containing compound2Absorbent for promoting reaction to generate H2Is moved in the direction of the adsorbent, and high-purity CO is obtained simultaneously after the adsorbent is regenerated2Can be directly trapped, sealed and utilized. The chemical looping hydrogen production technology can dissociate water to generate hydrogen under the assistance of an oxygen carrier, and the hydrogen can be kept at high purity without an additional purification process. The technology avoids the traditionThe disadvantage of methane steam reforming hydrogen production provides a new idea for developing a novel methane hydrogen production system, so that a system and a method are urgently needed to be developed, and the system and the method can realize the coupling of adsorption-enhanced steam reforming and chemical-looping hydrogen production.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a biogas hydrogen production system and a biogas hydrogen production method for a sewage treatment plant, which can realize the coupling of adsorption-enhanced steam reforming and chemical-looping hydrogen production.
In order to achieve the aim, the biogas hydrogen production system of the sewage treatment plant comprises an anaerobic fermentation tank, a desulfurization adsorption device, a nitrogen and oxygen removal device, a reduction reactor, a first separator, an oxidation reactor, a second separator, a calciner and a third separator;
the methane outlet of the anaerobic fermentation tank is communicated with the inlet of the reduction reactor through a desulfurization adsorption device and a nitrogen-oxygen removal device, the outlet of the reduction reactor is communicated with the inlet of the first separator, the solid outlet of the first separator is communicated with the inlet of the oxidation reactor, the outlet of the oxidation reactor is communicated with the inlet of the second separator, the solid outlet of the second separator is communicated with the inlet of the calciner, the outlet of the calciner is communicated with the inlet of the third separator, the solid outlet of the third separator is communicated with the inlet of the reduction reactor, and the outlet of the steam pipeline is communicated with the inlet of the reduction reactor and the inlet of the oxidation reactor.
The bottom outlet of the anaerobic fermentation tank is communicated with the inlet of the sludge tank.
The first separator, the second separator and the third separator are all cyclone separators.
The method for producing hydrogen by using the biogas of the sewage treatment plant comprises the following steps:
1) the oxidation state oxygen carrier and CaO absorbent enter a reduction reactor, the methane output by the anaerobic fermentation tank enters the reduction reactor, and the oxidation state oxygen carrier, the methane and the water vapor perform reduction reaction in the reduction reactor to generate reduction state oxygen carrier and CO2Gas and synthesis gas, wherein,CO2the gas is absorbed by CaO absorbent to generate CaCO3Reduction of CaCO output from the reactor3The reduced oxygen carrier and the synthesis gas enter a first separator for separation, the synthesis gas separated by the first separator is discharged, and CaCO separated by the first separator is discharged3The reduced oxygen carrier enters an oxidation reactor, and the reduced oxygen carrier and water vapor are subjected to oxidation reaction in the oxidation reactor to generate an oxidized oxygen carrier and hydrogen;
2) CaCO output from oxidation reactor3The oxygen carrier in oxidation state and the hydrogen enter a second separator for separation, wherein the separated hydrogen is discharged, and the separated CaCO3And the oxygen carrier in the oxidation state enters a calcinator for calcination, wherein CaCO3Decomposing at high temperature in the calcining process to generate CaO and CO2Gas, oxygen carrier in oxidation state output from calciner, CaO and CO2The gas enters a third separator for separation, wherein CO separated by the third separator2And discharging the gas, and feeding the oxidation state oxygen carrier and CaO separated by the third separator into a reduction reactor.
The reaction temperature of the reduction reactor is 500-800 ℃.
The reaction temperature of the oxidation reactor is 400-700 ℃.
The calcining temperature of the calciner is 800-1000 ℃.
The invention has the following beneficial effects:
during the specific operation of the sewage treatment plant biogas hydrogen production system and the sewage treatment plant biogas hydrogen production method, in a reduction reactor, an oxidation state oxygen carrier, biogas and steam are subjected to reduction reaction to generate a reduction state oxygen carrier and CO2Gas and syngas with CO2The gas is absorbed by CaO absorbent to generate CaCO3In the oxidation reactor, the reduction-state oxygen carrier and the steam are subjected to oxidation reaction to generate the oxidation-state oxygen carrier and the hydrogen so as to realize the coupling of adsorption-enhanced steam reforming and chemical-looping hydrogen production, and the high-purity hydrogen can be obtained without additional purification and separation steps so as to meet the market demand of hydrogen energy and improve the utilization value of the methane. At the same time, by coupling adsorption strengthening technology, promoteThe hydrogen yield in the steam reforming process and the hydrogen content in the synthesis gas are obviously increased, and the economic value of the synthesis gas is improved. Finally, the invention realizes low-cost carbon dioxide capture and separation while producing hydrogen from the biogas of a sewage treatment plant, and has good emission reduction effect.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Wherein, 1 is an anaerobic fermentation tank, 2 is a sludge tank, 3 is a desulfurization adsorption device, 4 is a nitrogen oxygen removal device, 5 is a reduction reactor, 6 is a first separator, 7 is an oxidation reactor, 8 is a second separator, 9 is a calcinator, and 10 is a third separator.
Detailed Description
The invention is described in further detail below with reference to the accompanying drawings:
referring to fig. 1, the biogas hydrogen production system of the sewage treatment plant according to the present invention includes an anaerobic fermentation tank 1, a desulfurization adsorption device 3, a nitrogen and oxygen removal device 4, a reduction reactor 5, a first separator 6, an oxidation reactor 7, a second separator 8, a calciner 9, and a third separator 10; the biogas outlet of the anaerobic fermentation tank 1 is communicated with the inlet of a reduction reactor 5 through a desulfurization adsorption device 3 and a nitrogen and oxygen removal device 4, the outlet of the reduction reactor 5 is communicated with the inlet of a first separator 6, the solid outlet of the first separator 6 is communicated with the inlet of an oxidation reactor 7, the outlet of the oxidation reactor 7 is communicated with the inlet of a second separator 8, the solid outlet of the second separator 8 is communicated with the inlet of a calciner 9, the outlet of the calciner 9 is communicated with the inlet of a third separator 10, the solid outlet of the third separator 10 is communicated with the inlet of the reduction reactor 5, and the outlet of a steam pipeline is communicated with the inlet of the reduction reactor 5 and the inlet of the oxidation reactor 7.
The bottom outlet of the anaerobic fermentation tank 1 is communicated with the inlet of the sludge tank 2; the first separator 6, the second separator 8 and the third separator 10 are all cyclone separators.
The method for producing hydrogen by using the biogas of the sewage treatment plant comprises the following steps:
1) the oxidation state oxygen carrier and the CaO absorbent enter into reduction reactionIn the reactor 5, the marsh gas output from the anaerobic fermentation tank 1 enters a reduction reactor 5, and in the reduction reactor 5, the oxidation state oxygen carrier, the marsh gas and the water vapor are subjected to reduction reaction to generate reduction state oxygen carrier and CO2Gas and synthesis gas, in which CO2The gas is absorbed by CaO absorbent to generate CaCO3Reduction of CaCO from the reactor 53The reduced oxygen carrier and the synthesis gas enter a first separator 6 for separation, the synthesis gas separated by the first separator 6 is discharged, and CaCO separated by the first separator 63The reduced oxygen carrier enters an oxidation reactor 7, and the reduced oxygen carrier and water vapor are subjected to oxidation reaction in the oxidation reactor 7 to generate an oxidized oxygen carrier and hydrogen;
2) CaCO from the oxidation reactor 73The oxygen carrier in oxidation state and the hydrogen enter a second separator 8 for separation, wherein the separated hydrogen is discharged, and the separated CaCO3And the oxygen carrier in oxidation state enters a calcinator 9 for calcination, wherein CaCO3Decomposing at high temperature in the calcining process to generate CaO and CO2Gases, oxygen carriers in the oxidized state, CaO and CO, output from the calciner 92The gas is separated in a third separator 10, wherein the CO is separated in the third separator 102The gas is discharged, and the oxygen carriers in the oxidation state and the CaO separated by the third separator 10 enter the reduction reactor 5.
The oxygen carrier comprises one or more of Fe-based, Co-based, Ni-based and Cu-based oxygen carriers; with SiC and Al2O3One or more inert carriers can be mixed for use.
Taking Fe-based oxygen carrier as an example, the reaction temperature of the reduction reactor 5 is 500-800 ℃, and the reaction involved in the reduction reactor 5 is as follows:
Fe3O4+CH4→3FeO+CO+2H2
2Fe3O4+CH4→6FeO+CO2+2H2
FeO+H2→Fe+H2O
FeO+CO→Fe+CO2
CH4+H2O→CO+3H2
CO+H2O→CO2+H2
CaO+CO2→CaCO3
the hydrogen content in the product synthetic gas reaches more than 97 percent, and the product synthetic gas can be used as a chemical raw material for synthesizing chemicals such as methanol, olefin, aromatic hydrocarbon and the like, and can also be further separated and purified to obtain high-purity hydrogen. The reaction temperature of the oxidation reactor 7 is 400-700 ℃, and the reaction involved in the oxidation reactor 7 is as follows:
Fe+H2O→FeO+H2
3FeO+H2O→Fe3O4+H2
because only one reaction of water dissociation occurs in the reactor, the purity of the product hydrogen can reach more than 99.9 percent, and the product hydrogen can be used as a hydrogen source to supply hydrogen for the market demand.
The calcining temperature of the calciner 9 is 800-1000 ℃, and the reaction involved in the calciner 9 is as follows:
CaCO3→CaO+CO2。
the high-purity CO2 obtained after calcination can be stored and used as a food additive or dry ice, and the like, can realize the capture and resource utilization of CO2, and has important significance for greenhouse gas emission reduction.
Claims (7)
1. A sewage treatment plant biogas hydrogen production system is characterized by comprising an anaerobic fermentation tank (1), a desulfurization adsorption device (3), a nitrogen and oxygen removal device (4), a reduction reactor (5), a first separator (6), an oxidation reactor (7), a second separator (8), a calciner (9) and a third separator (10);
the biogas outlet of the anaerobic fermentation tank (1) is communicated with the inlet of a reduction reactor (5) through a desulfurization adsorption device (3) and a nitrogen and oxygen removal device (4), the outlet of the reduction reactor (5) is communicated with the inlet of a first separator (6), the solid outlet of the first separator (6) is communicated with the inlet of an oxidation reactor (7), the outlet of the oxidation reactor (7) is communicated with the inlet of a second separator (8), the solid outlet of the second separator (8) is communicated with the inlet of a calciner (9), the outlet of the calciner (9) is communicated with the inlet of a third separator (10), the solid outlet of the third separator (10) is communicated with the inlet of the reduction reactor (5), and the outlet of a water vapor pipeline is communicated with the inlet of the reduction reactor (5) and the inlet of the oxidation reactor (7).
2. The biogas hydrogen production system of the sewage treatment plant according to claim 1, wherein the bottom outlet of the anaerobic fermentation tank (1) is communicated with the inlet of the sludge tank (2).
3. The sewage treatment plant biogas hydrogen production system according to claim 1, wherein the first separator (6), the second separator (8) and the third separator (10) are cyclone separators.
4. A method for producing hydrogen by using biogas from a sewage treatment plant is characterized by comprising the following steps:
1) the oxidation state oxygen carrier and CaO absorbent enter a reduction reactor (5), the marsh gas output by the anaerobic fermentation tank (1) enters the reduction reactor (5), and the oxidation state oxygen carrier, the marsh gas and the water vapor carry out reduction reaction in the reduction reactor (5) to generate the reduction state oxygen carrier and CO2Gas and synthesis gas, in which CO2The gas is absorbed by CaO absorbent to generate CaCO3Reduction of CaCO output from the reactor (5)3The reduced oxygen carrier and the synthesis gas enter a first separator (6) for separation, the synthesis gas separated by the first separator (6) is discharged, and CaCO separated by the first separator (6)3The reduced oxygen carrier enters an oxidation reactor (7), and in the oxidation reactor (7), the reduced oxygen carrier and water vapor are subjected to oxidation reaction to generate an oxidized oxygen carrier and hydrogen;
2) CaCO discharged from the oxidation reactor (7)3The oxygen carrier in oxidation state and the hydrogen enter a second separator (8) for separation, wherein the separated hydrogen is discharged, and the separated CaCO3And the oxygen carrier in the oxidation state enters a calcinator (9) for calcination, wherein CaCO3Decomposing at high temperature in the calcining process to generate CaO and CO2Gas, calciningThe oxidation state oxygen carrier, CaO and CO output by the device (9)2The gas enters a third separator (10) for separation, wherein CO separated by the third separator (10)2And discharging the gas, and feeding the oxidation state oxygen carriers and CaO separated by the third separator (10) into the reduction reactor (5).
5. The method for producing hydrogen by using biogas from a sewage treatment plant according to claim 4, wherein the reaction temperature of the reduction reactor (5) is 500-800 ℃.
6. The method for producing hydrogen by using biogas from a sewage treatment plant according to claim 4, wherein the reaction temperature of the oxidation reactor (7) is 400-700 ℃.
7. The method for producing hydrogen by using biogas from a sewage treatment plant according to claim 4, wherein the calcining temperature of the calciner (9) is 800-1000 ℃.
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| CN202010420542.XA CN111422830A (en) | 2020-05-18 | 2020-05-18 | Sewage treatment plant biogas hydrogen production system and method |
| PCT/CN2020/121186 WO2021232663A1 (en) | 2020-05-18 | 2020-10-15 | System and method for producing hydrogen from biogas in sewage treatment plant |
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| CN202010420542.XA CN111422830A (en) | 2020-05-18 | 2020-05-18 | Sewage treatment plant biogas hydrogen production system and method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113522933A (en) * | 2021-07-12 | 2021-10-22 | 深圳市深能环保东部有限公司 | Strong coupling cooperative treatment method for urban vein industrial park waste |
| WO2021232663A1 (en) * | 2020-05-18 | 2021-11-25 | 中国华能集团清洁能源技术研究院有限公司 | System and method for producing hydrogen from biogas in sewage treatment plant |
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| CN102858685A (en) * | 2010-02-01 | 2013-01-02 | 能源与环境解决方案参考有限公司 | Method And System For Producing Hydrogen From Carbon-containing Raw Material |
| CN103288048A (en) * | 2013-05-20 | 2013-09-11 | 大连理工大学 | Process for preparing hydrogen by strengthening chemical chain reforming in continuous catalytic adsorption manner via moving bed |
| CN103552983A (en) * | 2013-10-25 | 2014-02-05 | 西南石油大学 | CaO guided technology for producing hydrogen through steam reforming and chemical looping combustion of methane |
| CN108328576A (en) * | 2017-12-26 | 2018-07-27 | 华中科技大学 | A kind of co-generation unit based on chemical chain methane reforming process for making hydrogen |
| CN109233910A (en) * | 2018-11-07 | 2019-01-18 | 中石化南京工程有限公司 | A kind of system and method for the coal hydrogen based on chemical chain technology |
| CN212292791U (en) * | 2020-05-18 | 2021-01-05 | 中国华能集团清洁能源技术研究院有限公司 | Sewage treatment plant marsh gas hydrogen production system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2021232663A1 (en) * | 2020-05-18 | 2021-11-25 | 中国华能集团清洁能源技术研究院有限公司 | System and method for producing hydrogen from biogas in sewage treatment plant |
| CN113522933A (en) * | 2021-07-12 | 2021-10-22 | 深圳市深能环保东部有限公司 | Strong coupling cooperative treatment method for urban vein industrial park waste |
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