CN109233910B - System and method for preparing hydrogen from coal based on chemical chain technology - Google Patents
System and method for preparing hydrogen from coal based on chemical chain technology Download PDFInfo
- Publication number
- CN109233910B CN109233910B CN201811320665.5A CN201811320665A CN109233910B CN 109233910 B CN109233910 B CN 109233910B CN 201811320665 A CN201811320665 A CN 201811320665A CN 109233910 B CN109233910 B CN 109233910B
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- oxygen carrier
- reducer
- oxidizer
- air
- 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.)
- Active
Links
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 45
- 239000001257 hydrogen Substances 0.000 title claims abstract description 41
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 239000003245 coal Substances 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000005516 engineering process Methods 0.000 title claims abstract description 14
- 239000000126 substance Substances 0.000 title claims abstract description 13
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 51
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000001301 oxygen Substances 0.000 claims abstract description 50
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 41
- 239000007789 gas Substances 0.000 claims abstract description 36
- 239000007800 oxidant agent Substances 0.000 claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 16
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 16
- 238000002309 gasification Methods 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 230000003647 oxidation Effects 0.000 claims abstract description 7
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 40
- 239000007787 solid Substances 0.000 claims description 9
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- 239000004480 active ingredient Substances 0.000 claims 2
- 239000004615 ingredient Substances 0.000 claims 1
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000000446 fuel Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/725—Redox processes
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
The invention discloses a system and a method for preparing hydrogen from coal based on a chemical chain technology, wherein the method is that air enters an air separation unit to obtain pure oxygen; oxygen from the air separation unit and coal enter a gasification furnace to react to generate synthesis gas with main components of CO and H 2; the synthesis gas from the gasification furnace and the high-temperature oxygen carrier in the highest valence state from the air burner enter a reducer, the high-temperature oxygen carrier is reduced in the reducer, and the synthesis gas is oxidized into CO 2、H2 O and the like; the reduced oxygen carrier from the reducer and the steam from the heat exchanger enter the oxidizer, the reduced oxygen carrier is oxidized in the oxidizer, and the steam is reduced into hydrogen in a large part; the oxygen carrier in the oxidation state from the oxidizer and the air from the atmosphere enter an air burner where the oxygen carrier in the oxidation state is oxidized to the highest valence state and then sent to a reducer for reaction. The invention has the advantages of low cost, high energy conversion efficiency, environmental protection and energy saving.
Description
Technical Field
The invention relates to a system and a method for preparing hydrogen from coal based on a chemical chain technology, and belongs to the technical field of coal chemical industry.
Background
Hydrogen is a clean energy source and can be used as an alternative energy source for fossil fuels in the future. The byproduct of combustion is water only, hydrogen can meet the increasing energy demand, and is harmless to the environment.
Currently, most of the industrial scale hydrogen is derived from natural gas reforming, but the production of hydrogen from coal is a more economical option due to the ever-increasing price of natural gas.
The traditional coal hydrogen production technology has the technical route that the coal is directly gasified to generate synthetic gas (CO+H 2), and the synthetic gas generates hydrogen and CO 2 through a water gas shift reaction. Since the hydrogen produced by the water gas shift reaction contains a large amount of CO 2, it is necessary to separate CO 2 by low-temperature methanol washing and PSA units to obtain high-purity hydrogen. The addition of subsequent separation units to separate the CO 2 results in increased investment, reduced overall energy efficiency of the system, and only CO 2 at atmospheric pressure, and secondary pressurization has to be performed to transfer the CO 2 to the sequestration site and achieve capture, resulting in further reduction in energy efficiency.
Disclosure of Invention
The invention provides a system and a method for preparing hydrogen from coal based on a chemical chain technology, aiming at the technical problems, and the system and the method have the advantages of low cost, high energy conversion efficiency, environmental protection and energy saving.
The aim of the invention can be achieved by the following technical scheme:
A method for preparing hydrogen from coal based on chemical chain technology, which comprises the following steps:
(1) Pure oxygen and coal enter a gasification furnace to react to generate synthesis gas containing CO and H 2;
(2) The synthesis gas from the gasification furnace and the high-temperature oxygen carrier in the highest valence state from the air burner enter a reducer, the high-temperature oxygen carrier is reduced in the reducer, and the synthesis gas is oxidized to produce a mixture containing CO 2 and water vapor;
(3) The reduced oxygen carrier from the reducer and the water vapor from the third heat exchanger enter an oxidizer, the reduced oxygen carrier is oxidized in the oxidizer, and the water vapor is reduced into hydrogen in a majority;
(4) The oxygen carrier in the oxidation state from the oxidizer and the air from the atmosphere enter an air burner, and the oxygen carrier in the oxidation state is oxidized to the highest valence state in the air burner and then sent to a reducer for reaction;
(5) Desalted water from the boundary region is converted into water vapor after heat exchange by the first heat exchanger, the second heat exchanger and the third heat exchanger, one part of the water vapor from the third heat exchanger enters the oxidizer to react, and the other part of the water vapor is sent to the expander to do work after being overheated by the fourth heat exchanger;
(6) Cooling the product gas from the reducer through a second heat exchanger and a first condenser, and separating water to obtain high-concentration CO 2;
(7) The product gas from the oxidizer is cooled by a third heat exchanger and a second condenser and separated from water to obtain high-concentration H 2.
In the technical scheme of the invention, the active component of the oxygen carrier is Fe 2O3, and the particle size range is 0.5-5 mm; the inert component of the oxygen carrier is one or more of Al 2O3、TiO2 and YSZ; preferably: the mass ratio of the active component to the inert component in the oxygen carrier is 1-10: 1, a step of; further preferred is: the mass ratio of the active component to the inert component in the oxygen carrier is 1-5: 1.
The technical scheme of the invention is as follows: the operating temperature of the reducer is 600-1100 ℃, and the operating pressure is 0.1-4MPa; preferably, the operating temperature is 800-950 ℃ and the operating pressure is 2.5-3.5MPa.
The technical scheme of the invention is as follows: the mol ratio of oxygen carrier/synthesis gas in the reducer is 0.2-0.9: 1, a step of; preferably: the mol ratio of oxygen carrier/synthesis gas in the reducer is 0.5-0.9: 1.
The technical scheme of the invention is as follows: the operating temperature of the oxidizer is 650-850 ℃ and the operating pressure is 0.1-4MPa; preferably, the operating temperature is 700-800 ℃ and the operating pressure is 2.5-3.5MPa.
The technical scheme of the invention is as follows: the mol ratio of water vapor to oxygen carrier of the oxidizer is 0.5-1.5: 1.
The technical scheme of the invention is as follows: the operating temperature of the air burner is 650-1250 ℃ and the operating pressure is 0.1-4MPa; preferably, the operating temperature is 700-900 ℃ and the operating pressure is 2.5-3.5MPa.
The technical scheme of the invention is as follows: the weight ratio of oxygen carrier/air in the air burner is 10-30: 1, a step of; preferably: the weight ratio of oxygen carrier/air in the air burner is 15-30: 1.
A system for realizing the coal-to-hydrogen based on the chemical-looping technology, which comprises an air separation unit, a gasifier, a reducer, an oxidizer and an air burner;
the coal output pipeline and the air separation unit output pipeline are connected with a reducer through a gasifier, the solid output pipeline of an air burner is connected with the reducer, and the gas output end of the reducer is connected with a first condenser through a second heat exchanger in sequence; the solid output pipeline of the reducer and one output pipeline of the third heat exchanger are connected with the oxidizer, the gas output pipeline of the oxidizer is connected with the hydrogen compressor through the third heat exchanger, the second condenser and the hydrogen compressor in sequence, and the solid output pipeline of the oxidizer is connected with the air burner; the air burner is connected with the expansion machine through a fourth heat exchanger.
In the above system: the desalted water output pipeline from the boundary region is connected with the third heat exchanger through the first heat exchanger, the second heat exchanger and the third heat exchanger, and the other output pipeline connected with the third heat exchanger is connected with the fourth heat exchanger.
The gasification furnace is a coal water slurry furnace or a shell furnace or other similar furnace types.
The pressure in the technical scheme of the invention is absolute pressure.
The invention has the beneficial effects that:
Chemical looping hydrogen production is a novel high-efficiency hydrogen production technology, and by means of circulation of oxygen carriers, the chemical looping hydrogen production can realize step-by-step transfer of oxygen from air/water vapor to fuel. Because the air, the fuel and the water vapor respectively participate in the reaction in different reactors, the nitrogen of the air, the CO 2 generated by the fuel and the H 2 generated by the water vapor after the reaction are not affected, so that the enriched high-purity CO 2 and the enriched high-concentration H 2 can be directly obtained, and the gas separation and enrichment cost is reduced. The synthesis gas generated by the gasification furnace can be directly converted into CO 2, the water gas conversion unit can be omitted, the process flow is simplified, the energy conversion efficiency is improved, and the energy efficiency can be improved to 74% from 64% of the traditional coal hydrogen production technology route. In addition, the invention saves the equipment investment and the operation cost of units such as water gas shift reaction, low-temperature methanol washing, PSA and the like.
Drawings
FIG. 1 is a schematic diagram of an embodiment of a process for producing hydrogen from coal based on chemical looping technology.
Wherein: 1 is an air separation unit, 2 is a gasification furnace, 3 is a reducer, 4 is an oxidizer, 5 is an air burner, 6 is a first heat exchanger, 7 is a second heat exchanger, 8 is a third heat exchanger, 9 is a first condenser, 10 is a second condenser, 11 is a fourth heat exchanger, 12 is an expander, and 13 is a nitrogen compressor.
Detailed Description
The invention is further illustrated below with reference to examples, but the scope of the invention is not limited thereto:
A system for preparing hydrogen from coal based on chemical chain technology comprises an air separation unit (1), a gasification furnace (2), a reducer (3), an oxidizer (4) and an air burner (5); the coal output pipeline and the air separation unit (1) are connected with the reducer (3) through the gasifier (2), the solid output pipeline of the air burner (5) is connected with the reducer (3), and the gas output end of the reducer (3) is connected with the first condenser (9) through the second heat exchanger (7) in sequence; the solid output pipeline of the reducer (3) and one output pipeline of the third heat exchanger (3) are connected with the oxidizer (4), the gas output pipeline of the oxidizer (4) is connected with the hydrogen compressor (13) through the third heat exchanger (8), the second condenser (10) in sequence, and the solid output pipeline of the oxidizer (4) is connected with the air burner (5); the air burner (5) is connected with the expander (12) through a fourth heat exchanger (11). The desalted water output pipeline from the boundary region is connected with a third heat exchanger (8) through a first heat exchanger (6), a second heat exchanger (7), and the other output pipeline connected with the third heat exchanger (8) is connected with a fourth heat exchanger (11).
The method for preparing hydrogen from coal by utilizing the system based on the chemical chain technology comprises the following steps:
the received base analysis of a coal species is as follows (wt%):
11.88% of ash; elemental carbon: 74.69%; elemental hydrogen: 4.98%; elemental nitrogen: 1.23%; elemental sulfur: 0.73%; elemental oxygen: 6.49%. The high-order heating value of the coal is 7832W.
The gasification furnace is a shell furnace, the coal flow entering the furnace is 1kg/h, the oxygen flow from the air separation unit is 0.86kg/h, the pressure of the synthesis gas after reaction exiting the shell furnace is 30atm, the temperature is 600 ℃, the flow is 0.0939kmol/h, and the general components are as follows:
The synthesis gas from the gasifier and the oxidized oxygen carrier enter the reducer in countercurrent (operating pressure of the reducer is 30atm, operating temperature is 897 ℃), the oxidized oxygen carrier flow is 0.0657kmol/H, the temperature is 750 ℃, the reduced oxygen carrier (0.0657 kmol/H,897 ℃) after reaction enters the oxidizer (operating pressure of the oxidizer is 30atm, operating temperature is 782 ℃), the gas products from the reducer are mainly CO 2 and H 2 O, and the CO 2 product flow with the temperature of 25 ℃, the flow rate of 2.57kg/H and the purity of 99.5% is obtained after cooling and separating water by the heat exchanger 2 and the condenser 1.
The desalted water from the boundary region is heated by a heat exchanger 1, a heat exchanger 2 and a heat exchanger 3 to obtain 300 ℃ water vapor, a part of the water vapor from the heat exchanger 3 enters an oxidizer to react with a reduced oxygen carrier, wherein the flow rate of the water vapor entering the oxidizer is 1.051kg/H, the temperature is 300 ℃, after the reaction in the oxidizer is finished, gas products (mainly H 2 O and H 2) are cooled by the heat exchanger 3 and a condenser 2, water is separated, high-purity hydrogen is obtained, and a hydrogen product with the pressure of 165atm and the flow rate of 0.148kg/H is obtained after the hydrogen product is compressed by a hydrogen compressor.
The oxidation state oxygen carrier (10.155 kg/h) from the oxidizer and the air (0.51 kg/h) from the boundary zone enter an air burner (air reactor operating temperature 750 ℃, air reactor operating pressure 30 atm) to react, and the highest valence state oxygen carrier (10.512 kg/h) obtained after the reaction enters the reducer again to circulate.
The water vapor from the heat exchanger 3 is superheated by the heat exchanger 4 and enters the expander to apply work, wherein one part of the work is used for an air compressor (344W) of the air separation unit, and the other part of the work is used for a hydrogen compressor (222W).
The active components of the oxygen carrier are Fe 2O3, the inert components are TiO 2 and Al 2O3, the mass specific gravity of the three components is 70%, 15% and 15%, and the particle size of the oxygen carrier is 5mm.
If the hydrogen generation efficiency is defined as the high-order heating value of hydrogen divided by the high-order heating value of coal, the hydrogen generation efficiency is 74% according to the process route of the present embodiment; according to the traditional coal gasification and water gas conversion technical route, the hydrogen generation efficiency is 64%, so that the invention can improve the hydrogen generation efficiency by 10 percent, thereby improving the energy utilization efficiency.
Claims (12)
1. A method for preparing hydrogen from coal based on chemical chain technology is characterized by comprising the following steps: the method comprises the following steps:
(1) Pure oxygen and coal enter a gasification furnace to react to generate synthesis gas containing CO and H 2;
(2) The synthesis gas from the gasification furnace and the high-temperature oxygen carrier in the highest valence state from the air burner enter a reducer, the high-temperature oxygen carrier is reduced in the reducer, and the synthesis gas is oxidized to produce a mixture containing CO 2 and water vapor;
(3) The reduced oxygen carrier from the reducer and the water vapor from the third heat exchanger enter an oxidizer, the reduced oxygen carrier is oxidized in the oxidizer, and the water vapor is reduced into hydrogen in a majority;
(4) The oxygen carrier in the oxidation state from the oxidizer and the air from the atmosphere enter an air burner, and the oxygen carrier in the oxidation state is oxidized to the highest valence state in the air burner and then sent to a reducer for reaction;
(5) Desalted water from the boundary region is converted into water vapor after heat exchange by the first heat exchanger, the second heat exchanger and the third heat exchanger, one part of the water vapor from the third heat exchanger enters the oxidizer to react, and the other part of the water vapor is sent to the expander to do work after being overheated by the fourth heat exchanger;
(6) Cooling the product gas from the reducer through a second heat exchanger and a first condenser, and separating water to obtain high-concentration CO 2;
(7) Cooling the product gas from the oxidizer by a third heat exchanger and a second condenser, and separating water to obtain high-concentration H 2;
The oxygen carrier consists of an active ingredient and an inert ingredient, wherein the active ingredient of the oxygen carrier is Fe 2O3, and the particle size range of the oxygen carrier is 0.5-5 mm; the inert component of the oxygen carrier is one or more of Al 2O3、TiO2 and YSZ; the mass ratio of the active component to the inert component in the oxygen carrier is 1-5: 1, a step of;
The system for realizing the method comprises an air separation unit (1), a gasification furnace (2), a reducer (3), an oxidizer (4) and an air burner (5),
The coal output pipeline and the air separation unit (1) are connected with the reducer (3) through the gasifier (2), the solid output pipeline of the air burner (5) is connected with the reducer (3), and the gas output end of the reducer (3) is connected with the first condenser (9) through the second heat exchanger (7) in sequence; the solid output pipeline of the reducer (3) and one output pipeline of the third heat exchanger (8) are connected with the oxidizer (4), the gas output pipeline of the oxidizer (4) is connected with the hydrogen compressor (13) through the third heat exchanger (8), the second condenser (10) in sequence, and the solid output pipeline of the oxidizer (4) is connected with the air burner (5); the air burner (5) is connected with the expander (12) through a fourth heat exchanger (11);
The desalted water output pipeline from the boundary region is connected with a third heat exchanger (8) through a first heat exchanger (6), a second heat exchanger (7), and the other output pipeline connected with the third heat exchanger (8) is connected with a fourth heat exchanger (11).
2. The method according to claim 1, characterized in that: the operating temperature of the reducer is 600-1100 ℃, and the operating pressure is 0.1-4Mpa.
3. The method according to claim 2, characterized in that: the operating temperature of the reducer is 800-950 ℃ and the operating pressure is 2.5-3.5MPa.
4. The method according to claim 1, characterized in that: the mol ratio of oxygen carrier/synthesis gas in the reducer is 0.2-0.9: 1.
5. The method according to claim 4, wherein: the mol ratio of oxygen carrier/synthesis gas in the reducer is 0.5-0.9: 1.
6. The method according to claim 1, characterized in that: the operating temperature of the oxidizer is 650-850 ℃ and the operating pressure is 0.1-4MPa.
7. The method according to claim 6, wherein: the operating temperature is 700-800 ℃, and the operating pressure is 2.5-3.5MPa.
8. The method according to claim 1, characterized in that: the mol ratio of water vapor to oxygen carrier of the oxidizer is 0.5-1.5: 1.
9. The method according to claim 1, characterized in that: the operating temperature of the air burner is 650-1250 ℃ and the operating pressure is 0.1-4MPa.
10. The method according to claim 9, wherein: the operating temperature of the air burner is 700-900 ℃ and the operating pressure is 2.5-3.5MPa.
11. The method according to claim 1, characterized in that: the weight ratio of oxygen carrier/air in the air burner is 10-30: 1.
12. The method according to claim 11, wherein: the weight ratio of oxygen carrier/air in the air burner is 15-30: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811320665.5A CN109233910B (en) | 2018-11-07 | 2018-11-07 | System and method for preparing hydrogen from coal based on chemical chain technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811320665.5A CN109233910B (en) | 2018-11-07 | 2018-11-07 | System and method for preparing hydrogen from coal based on chemical chain technology |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109233910A CN109233910A (en) | 2019-01-18 |
| CN109233910B true CN109233910B (en) | 2024-06-18 |
Family
ID=65077260
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811320665.5A Active CN109233910B (en) | 2018-11-07 | 2018-11-07 | System and method for preparing hydrogen from coal based on chemical chain technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109233910B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111422830A (en) * | 2020-05-18 | 2020-07-17 | 中国华能集团清洁能源技术研究院有限公司 | Sewage treatment plant biogas hydrogen production system and method |
| CN115432667A (en) * | 2022-08-24 | 2022-12-06 | 中国大唐集团科学技术研究总院有限公司华东电力试验研究院 | Biomass gasification-chemical looping hydrogen production device and method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105385473A (en) * | 2015-11-11 | 2016-03-09 | 中国科学院山西煤炭化学研究所 | Coal hydrogen and methane process based on chemical-looping gasification |
| CN209113821U (en) * | 2018-11-07 | 2019-07-16 | 中石化南京工程有限公司 | A kind of system of the coal hydrogen based on chemical chain technology |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103972559A (en) * | 2014-05-09 | 2014-08-06 | 东南大学 | Method and device for biomass combined cycle power generation and carbon dioxide separation |
-
2018
- 2018-11-07 CN CN201811320665.5A patent/CN109233910B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105385473A (en) * | 2015-11-11 | 2016-03-09 | 中国科学院山西煤炭化学研究所 | Coal hydrogen and methane process based on chemical-looping gasification |
| CN209113821U (en) * | 2018-11-07 | 2019-07-16 | 中石化南京工程有限公司 | A kind of system of the coal hydrogen based on chemical chain technology |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109233910A (en) | 2019-01-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101285004B (en) | Multifunctional energy resource system | |
| US10227901B2 (en) | Methanation method and power plant comprising CO2 methanation of power plant flue gas | |
| JP5820801B2 (en) | Tail gas recycling method and apparatus | |
| US20140377158A1 (en) | Chemical looping integration with a carbon dioxide gas purification unit | |
| CN108729965B (en) | Power generation system combining partial oxygen-enriched combustion of calcium-based chain and CO 2 Trapping method | |
| Romano et al. | Long-term coal gasification-based power plants with near-zero emissions. Part A: Zecomix cycle | |
| CN105385473A (en) | Coal hydrogen and methane process based on chemical-looping gasification | |
| CN112079333B (en) | Chain reaction hydrogen production system and hydrogen production method | |
| CN109233910B (en) | System and method for preparing hydrogen from coal based on chemical chain technology | |
| CN103045308B (en) | Power generation method and system based on step conversion of hydrocarbon components of coal | |
| CN101993730B (en) | Multifunctional energy system based on appropriate conversion of chemical energy of fossil fuel | |
| JP2024502731A (en) | Smart hydrogen production for DRI production | |
| JPH04244504A (en) | Carbon dioxide recovery type coal thermal power system | |
| JP2016530983A (en) | Method for sustainable energy generation in a power plant with a solid oxide fuel cell | |
| CN104987891B (en) | A kind of alternative fuel based on coal hydrocarbon component classification gasification/chemical products production system | |
| CN209113821U (en) | A kind of system of the coal hydrogen based on chemical chain technology | |
| CN115651714A (en) | Device and method for gasification conversion of low-calorific-value fuel | |
| WO2003080503A1 (en) | Method for producing syngas with recycling of water | |
| CN107151720A (en) | A kind of Lurgi gasifying gas converts the system and method for producing DRI through steam | |
| CN207002777U (en) | A kind of Lurgi gasifying gas converts the device of production DRI through steam | |
| CN116334326B (en) | Whole-process systematic carbon reduction method for steel and casting | |
| CN219174451U (en) | Device for gasifying and converting low-calorific-value fuel | |
| Gupta et al. | Chemical looping combustion of coal | |
| JPH0491324A (en) | Carbon dioxide recovering type thermal power generation system | |
| CN217418188U (en) | System for preparing methanol and co-producing hydrogen from synthesis gas by integrating chemical-looping coke oven gas reforming |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |