CN115818643A - Thermochemical CO 2 Interactive double-fixed-bed device and process for chemical chain conversion - Google Patents
Thermochemical CO 2 Interactive double-fixed-bed device and process for chemical chain conversion Download PDFInfo
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- CN115818643A CN115818643A CN202211581350.2A CN202211581350A CN115818643A CN 115818643 A CN115818643 A CN 115818643A CN 202211581350 A CN202211581350 A CN 202211581350A CN 115818643 A CN115818643 A CN 115818643A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 130
- 239000000126 substance Substances 0.000 title claims abstract description 42
- 230000002452 interceptive effect Effects 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims abstract description 15
- 239000012429 reaction media Substances 0.000 claims abstract description 41
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000001301 oxygen Substances 0.000 claims abstract description 4
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 4
- 239000002245 particle Substances 0.000 claims abstract description 4
- 239000007787 solid Substances 0.000 claims abstract description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 48
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 39
- 239000001257 hydrogen Substances 0.000 claims description 39
- 229910052739 hydrogen Inorganic materials 0.000 claims description 39
- 229910044991 metal oxide Inorganic materials 0.000 claims description 39
- 150000004706 metal oxides Chemical class 0.000 claims description 39
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 24
- 239000001569 carbon dioxide Substances 0.000 claims description 24
- 239000002184 metal Substances 0.000 claims description 22
- 229910052751 metal Inorganic materials 0.000 claims description 22
- 239000007789 gas Substances 0.000 claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 230000009977 dual effect Effects 0.000 claims description 4
- 125000004122 cyclic group Chemical group 0.000 claims description 3
- 238000011278 co-treatment Methods 0.000 claims 1
- 238000009434 installation Methods 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 12
- 230000001105 regulatory effect Effects 0.000 description 4
- 239000013589 supplement Substances 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- 229910020599 Co 3 O 4 Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
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Abstract
The invention belongs to the technical field of carbon conversion and utilization, and particularly relates to thermochemical CO 2 An interactive double fixed bed device and a process for chemical chain conversion. The invention provides an interactive double fixed bed device comprising CO 2 Chemical looping conversion system and circulating heat system, wherein, CO 2 The chemical chain conversion system comprises a first fixed bed reaction device internally provided with a plurality of layers of reaction media and a second fixed bed reaction device internally provided with a plurality of layers of reaction media, wherein the plurality of layers of reaction media are honeycomb-shaped solid oxygen carrier particles. On one hand, the alternative CO is realized by the tangential control operation of the valve 2 Continuous conversion, simple device, good stability and remarkable operability. On the other hand, the heat of the high-temperature product and the heat generated by the exothermic reaction can be recycled, and the energy utilization rate is high.
Description
Technical Field
The invention belongs to the technical field of carbon conversion and utilization, and particularly relates to thermochemical CO 2 An interactive double fixed bed device and a process for chemical chain conversion.
Background
China is the world with the largest carbon dioxide emission, the emission accounts for 30% of the world, and is also the world with the largest high-carbon carbide energy consumption, and coal accounts for more than 50% of the world total consumption. China already establishes a carbon peak carbon neutralization target. That is, the carbon dioxide emission in china peaked 2030 ago, and the effort was to achieve carbon neutralization 2060 ago. The method aims at improving the carbon emission statistical accounting system, perfecting the carbon emission right market trading system and improving the carbon exchange capacity of the ecological system. Therefore, in order to meet the significant demand of dual carbon targets, it is necessary to develop a carbon capture, utilization and sequestration (CCUS) technology to convert it into a useful product for utilization, and reduce the environmental pollution caused by carbon emission, so that the climate change can be slowed down.
CCUS technical system consisting of CO 2 Capture of, CO 2 Transport and captured CO 2 And then the process of reuse or safe sealing is formed. One has to mention the project of Petra Nova Carbon Capture in the United states, which is the largest CCUS project in the world, with capital expenditure exceeding 10 billion dollars and annual Capture of 140 million tons of CO 2 And the oil is transported to an old oil field West Ranch (1938) which is 100 kilometers away for oil displacement. Project investors have made measurements before shipping in 2017, month 1, and in order to maintain their normal operation, the oil price must be kept at $ 75/barrel to reach the profit equilibrium point. While the oil prices were substantially under $ 75 in the last five years, the project was shut down in 2021, month 1, day 29 for economic reasons. Therefore, the implementation of the CCUS project must be economically sustainable as an important consideration.
Disclosure of Invention
This project proposes a thermochemical CO 2 An interactive double-fixed-bed device and a process technology for chemical-looping conversion are environment-friendly, efficiently convert carbon dioxide into CO with high added value by thermochemistry, have high reaction rate, and achieve CO by switching control of a valve 2 And (4) converting uninterruptedly. The specific technical scheme is as follows:
a first aspect of the invention provides thermochemical CO 2 Interactive double fixed bed apparatus for chemical looping conversion comprising CO 2 Chemical looping conversion systems and cyclic thermal systems;
the CO is 2 The chemical chain conversion system comprises a first fixed bed reaction device 1 internally provided with a plurality of layers of reaction media 11 and a second fixed bed reaction device 2 internally provided with a plurality of layers of reaction media 11, wherein the plurality of layers of reaction media 11 are honeycomb-shaped solid oxygen carrier particles;
wherein, the outlet of the carbon dioxide storage tank 12 is communicated with the inlet of the first fixed bed reaction device 1 through a sixth throttling valve 8, and the outlet of the first fixed bed reaction device 1 is communicated with the inlet of the first condenser 24 through a second throttling valve 4; the outlet of the carbon dioxide storage tank 12 is communicated with the inlet of the second fixed bed reaction device 2 through an eighth throttling valve 10, and the outlet of the second fixed bed reaction device 2 is communicated with the inlet of the first condenser 24 through a fourth throttling valve 6;
the outlet of the hydrogen storage tank 13 is communicated with the inlet of the first fixed bed reaction device 1 through a fifth throttling valve 7, and the outlet of the first fixed bed reaction device 1 is communicated with the inlet of the second condenser 25 through a first throttling valve 3; the outlet of the hydrogen storage tank 13 is communicated with the inlet of the second fixed bed reaction device 2 through a seventh throttling valve 9, and the outlet of the second fixed bed reaction device 2 is communicated with the inlet of a second condenser 25 through a third throttling valve 5;
the circulating heat system comprises a first circulating heat exchange system 22, and the first circulating heat exchange system 22 comprises a first condenser 24, a second condenser 25, a heat exchanger 26 and a second circulating pump 28 which are communicated through heat exchange pipelines.
Preferably, the circulating heat system further comprises a second circulating heat exchange system 23, and the second circulating heat exchange system 23 comprises the first fixed bed reaction device 1, a first circulating pump 27, a heat exchanger 26 and a second fixed bed reaction device 2 which are communicated through heat exchange pipes.
Further, the first heat exchange medium tank 20 is connected with a second circulating heat exchange system 23, and the second heat exchange medium tank 21 is connected with the first circulating heat exchange system 22, so as to supplement the heat exchange medium.
Further, the heat exchanger 26 is used for heating the heat exchange medium in the second circulation heat exchange system 23.
Further, the tank bodies of the first fixed bed reaction device 1 and the second fixed bed reaction device 2 are provided with throttle valves for adjusting the flow rate of the heat exchange medium.
Further, a high valence metal oxide is charged into the multi-layer reaction medium 11 in the fixed bed reaction device to which hydrogen is supplied first, and a low valence metal oxide or a simple metal is charged into the multi-layer reaction medium 11 in the other fixed bed reaction device.
A second aspect of the invention provides thermochemical CO 2 A chemical looping conversion process is carried out based on the interactive double fixed bed apparatus provided in the first aspect of the invention, specifically, a carbon dioxide storage tank 12 supplies CO to one of the fixed bed reaction apparatuses 2 The sensible heat of the generated CO gas is cooled by the first condenser 24 after the reaction with the low-valence metal oxide or the metal simple substance in the multilayer reaction medium 11; the hydrogen storage tank 13 supplies hydrogen to the other fixed bed reaction device, reacts with the high valence metal oxide in the multilayer reaction medium 11 to generate high temperature water vapor, and the high temperature water vapor is sent to the heat exchange pipeline after heat exchange through the second condenser 25; after the conversion of the multi-layer reaction medium 11 is completed, the throttle valves are adjusted, and the carbon dioxide storage tank 12 and the hydrogen storage tank 13 are respectively switched to different fixed bed reaction devices to supply CO 2 And hydrogen.
More specifically, the first throttle valve 3, the fourth throttle valve 6, the fifth throttle valve 7, the eighth throttle valve 10 are opened, the second throttle valve 4, the third throttle valve 5, the sixth throttle valve 8, the seventh throttle valve 9 are closed, and the carbon dioxide storage tank 12 supplies CO to the second fixed bed reactor 2 2 The sensible heat of the generated CO gas is cooled by the first condenser 24 after the reaction with the low-valence metal oxide or the metal simple substance in the multilayer reaction medium 11; the hydrogen storage tank 13 supplies hydrogen to the first fixed bed reactor 1, and reacts with the high valence metal oxide in the multi-layer reaction medium 11 to generate high temperature steam, which is sent to the heat exchange pipeline after heat exchange by the second condenser 25.
Further, the low valence metal oxide or the simple metal in the second fixed bed reactor 2 is oxidized to generate high valence metal oxygenAfter the high valence metal oxide in the first fixed bed reactor 1 is reduced to low valence metal oxide or metal simple substance, the first throttle valve 3, the fourth throttle valve 6, the fifth throttle valve 7 and the eighth throttle valve 10 are closed, the second throttle valve 4, the third throttle valve 5, the sixth throttle valve 8 and the seventh throttle valve 9 are opened, and the hydrogen in the hydrogen storage tank 13 enters the CO in the second fixed bed reactor 2 and the carbon dioxide storage tank 12 2 The reaction is repeated in the first fixed bed reactor 1.
Further, the generated CO gas is used for storage and utilization.
The invention has the beneficial effects that: on one hand, the interactive double-fixed bed device provided by the invention realizes the alternative CO through the tangential control operation of the valve 2 Continuous conversion, simple device, good stability and remarkable operability. On the other hand, the heat of the high-temperature product and the heat generated by the exothermic reaction can be recycled, and the energy utilization rate is high. Compared with the traditional reverse water gas shift reaction, the yield of CO can be improved by more than 6 times.
Drawings
FIG. 1 is a thermochemical CO of the invention 2 Schematic structure of interactive double fixed bed device for chemical chain conversion.
Description of reference numerals: 1-a first fixed bed reaction device, 2-a second fixed bed reaction device, 3-a first throttle valve, 4-a second throttle valve, 5-a third throttle valve, 6-a fourth throttle valve, 7-a fifth throttle valve, 8-a sixth throttle valve, 9-a seventh throttle valve, 10-an eighth throttle valve, 11-a multi-layer reaction medium, 12-a carbon dioxide storage tank, 13-a hydrogen storage tank, 14-a ninth throttle valve, 15-a tenth throttle valve, 16-an eleventh throttle valve, 17-a twelfth throttle valve, 18-a thirteenth throttle valve, 19-a fourteenth throttle valve, 20-a first heat exchange medium tank, 21-a second heat exchange medium tank, 22-a first circulating heat exchange system, 23-a second circulating heat exchange system, 24-a first condenser, 25-a second condenser, 26-a heat exchanger, 27-a first circulating pump, 28-a second circulating pump, 29-a fifteenth throttle valve, 30-a sixteenth throttle valve.
Detailed Description
The invention provides thermochemical CO 2 The invention is further illustrated by the following examples. The terms "first," "second," and the like in the description and claims of the present invention and in the preceding drawings are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order.
The first aspect of the invention provides a thermochemical CO 2 An interactive dual fixed bed apparatus for chemical looping conversion, as shown in FIG. 1, includes CO 2 Chemical chain conversion systems and cyclic thermal systems.
For the CO 2 The chemical chain conversion system comprises a first fixed bed reaction device 1 with a plurality of layers of reaction media 11 arranged inside and a second fixed bed reaction device 2 with a plurality of layers of reaction media 11 arranged inside, wherein the plurality of layers of reaction media 11 are honeycomb-shaped solid oxygen carrier particles.
Two throttle valves are arranged at the inlet and outlet of the first fixed bed reaction device 1 and the second fixed bed reaction device 2. Specifically, the inlet of the first fixed bed reactor 1 is provided with a fifth throttling valve 7 and a sixth throttling valve 8, and the outlet is provided with a first throttling valve 3 and a second throttling valve 4; the inlet of the second fixed bed reaction device 2 is provided with a seventh throttling valve 9 and an eighth throttling valve 10, and the outlet is provided with a third throttling valve 5 and a fourth throttling valve 6.
The outlet of the carbon dioxide storage tank 12 is communicated with the inlet of the first fixed bed reaction device 1 through a sixth throttling valve 8, and the outlet of the first fixed bed reaction device 1 is communicated with the inlet of the first condenser 24 through a second throttling valve 4; the outlet of the carbon dioxide storage tank 12 is communicated with the inlet of the second fixed bed reaction device 2 through the eighth throttling valve 10, and the outlet of the second fixed bed reaction device 2 is communicated with the inlet of the first condenser 24 through the fourth throttling valve 6.
The outlet of the hydrogen storage tank 13 is communicated with the inlet of the first fixed bed reaction device 1 through a fifth throttling valve 7, and the outlet of the first fixed bed reaction device 1 is communicated with the inlet of the second condenser 25 through a first throttling valve 3; the outlet of the hydrogen storage tank 13 is communicated with the inlet of the second fixed bed reaction device 2 through a seventh throttling valve 9, and the outlet of the second fixed bed reaction device 2 is communicated with the inlet of the second condenser 25 through a third throttling valve 5.
Further, a high valence metal oxide is charged into the multi-layer reaction medium 11 in the fixed bed reaction device to which hydrogen is supplied first, and a low valence metal oxide or a simple metal is charged into the multi-layer reaction medium 11 in the other fixed bed reaction device. Wherein the higher valent metal oxide includes, but is not limited to, fe 3 O 4 、CuO、Mn 3 O 4 、Co 3 O 4 Any one or more of the above components can be combined with hydrogen to perform oxidation-reduction reaction; wherein, the lower valence metal oxide or metal simple substance includes but not limited to any one or more combination of FeO, cu, mnO and CoO, and can be combined with CO 2 And carrying out oxidation-reduction reaction. Based on the design idea of the serial double fluidized bed device, the high-valence metal oxide, the low-valence metal oxide or the metal simple substance are preferably the same metal, so as to be recycled.
In operation, the carbon dioxide storage tank 12 supplies CO to one of the fixed bed reactors 2 And reacts with the lower valence metal oxide or the metal simple substance in the multilayer reaction medium 11 to generate CO gas, sensible heat of the CO gas is cooled by the first condenser 24, and the cooled CO gas is stored. The hydrogen storage tank 13 supplies hydrogen to the other fixed bed reaction device, reacts with the high valence metal oxide in the multilayer reaction medium 11 to generate high temperature water vapor, and the high temperature water vapor is sent to the heat exchange pipeline after heat exchange through the second condenser 25; after the conversion of the multi-layer reaction medium 11 is completed, the throttle valves are adjusted, and the carbon dioxide storage tank 12 and the hydrogen storage tank 13 are respectively switched to different fixed bed reaction devices to supply CO 2 And hydrogen.
As an example, a high valence metal oxide is charged in the multi-layer reaction medium 11 of the first fixed bed reaction device 1, and a low valence metal oxide or a simple metal is charged in the multi-layer reaction medium 11 of the second fixed bed reaction device 2. In operation, the first throttle valve 3, the fourth throttle valve 6, the fifth throttle valve 7, and the eighth throttle valve 10 are opened, the second throttle valve 4, the third throttle valve 5, the sixth throttle valve 8, and the seventh throttle valve 9 are closed, and the carbon dioxide storage tank 12 supplies CO to the second fixed bed reactor 2 2 With lower valency in the multilayer reaction medium 11The sensible heat of the generated CO gas is cooled by the first condenser 24; the hydrogen storage tank 13 supplies hydrogen to the first fixed bed reactor 1, and reacts with the high valence metal oxide in the multi-layer reaction medium 11 to generate high temperature steam, which is sent to the heat exchange pipeline after heat exchange by the second condenser 25. After the low-valence metal oxide in the second fixed bed reaction device 2 is oxidized to generate high-valence metal oxide, the high-valence metal oxide in the first fixed bed reaction device 1 is reduced to low-valence metal, the first throttle valve 3, the fourth throttle valve 6, the fifth throttle valve 7 and the eighth throttle valve 10 are closed, the second throttle valve 4, the third throttle valve 5, the sixth throttle valve 8 and the seventh throttle valve 9 are opened, hydrogen in the hydrogen storage tank 13 enters the second fixed bed reaction device 2, and CO in the carbon dioxide storage tank 12 2 The reaction is repeated in the first fixed bed reactor 1.
For the circulating heat system, the circulating heat system comprises a first circulating heat exchange system 22, and the first circulating heat exchange system 22 comprises a first condenser 24, a second condenser 25, a heat exchanger 26 and a second circulating pump 28 which are communicated through heat exchange pipelines. The first condenser 24 and the second condenser 25 exchange heat of high-temperature CO and water vapor for heat exchange media in the pipelines, the heat exchange media are heated respectively in the first condenser 24 and the second condenser 25 and provide heat for the second fixed bed reaction device 2 through the heat exchanger 26, and the heat exchange media after heat exchange are sent back to the first condenser 24 and the second condenser 25 through the second circulating pump 28 to continuously exchange heat, so that heat circulation is formed sequentially.
Specifically, by designing heat exchange tubes in the multi-layer reaction medium 11 of the second fixed bed reaction device 2, the heated heat exchange medium provides heat for the reaction through the heat exchange tubes.
Preferably, the second heat exchange medium tank 21 is connected to the first circulating heat exchange system 22, and a sixteenth throttling valve 30 is designed at an outlet of the second heat exchange medium tank 21 for regulating and controlling the second heat exchange medium tank 21 to supplement the heat exchange medium to the first circulating heat exchange system 22.
Preferably, the tank of the second fixed bed reactor 2 is provided with throttle valves, such as a ninth throttle valve 14, a tenth throttle valve 15 and an eleventh throttle valve 16, which are uniformly spaced and are used for regulating the flow of the heat exchange medium entering the heat exchange tubes of the second fixed bed reactor 2.
In other preferred embodiments, the circulating heat system further comprises a second circulating heat exchange system 23, and the second circulating heat exchange system 23 comprises the first fixed bed reaction device 1, the first circulating pump 27, the heat exchanger 26 and the second fixed bed reaction device 2 which are communicated through heat exchange pipes. Specifically, heat exchange pipes are designed in the multilayer reaction medium 11 of the first fixed bed reaction device 1 and the multilayer reaction medium 11 of the second fixed bed reaction device 2, and the heat exchange pipes are connected in series with the first fixed bed reaction device 1, the first circulation pump 27, the heat exchanger 26 and the second fixed bed reaction device 2 to form the second circulation heat exchange system 23. Specifically, the outlet pipeline of the first circulating pump 27 may be directly connected to the heat exchange pipeline in the second fixed bed reactor 2, or may be communicated with the heat exchanger 26 and then enter the second fixed bed reactor 2.
Preferably, the first heat exchange medium storage tank 20 is connected with the second circulating heat exchange system 23, and a fifteenth throttling valve 29 is designed at the outlet of the first heat exchange medium storage tank 20 for regulating and controlling the first heat exchange medium storage tank 20 to supplement the heat exchange medium to the second circulating heat exchange system 23.
Preferably, flow valves are arranged in the tank body of the first fixed bed reactor 1, such as a twelfth throttling valve 17, a thirteenth throttling valve 18 and a fourteenth throttling valve 19 which are uniformly arranged at intervals and used for regulating the flow of the heat exchange medium entering the heat exchange pipelines in the first fixed bed reactor 1.
The interactive dual fixed bed apparatus provided by the first aspect of the invention achieves heat recovery through two cycles and CO 2 The chemical looping conversion can realize the opening and closing control of the first throttle valve 3, the second throttle valve 4, the third throttle valve 5, the fourth throttle valve 6, the fifth throttle valve 7, the sixth throttle valve 8, the seventh throttle valve 9 and the eighth throttle valve 10 to realize CO 2 The conversion to CO is continuously carried out, and the metal simple substance and the oxide thereof can be recycled.
A second aspect of the invention provides thermochemical CO 2 Chemical chain conversion process, said process being based on the first aspect of the inventionThe surface-provided interactive double fixed bed device.
As an example of concrete operation, the first throttle valve 3, the fourth throttle valve 6, the fifth throttle valve 7, the eighth throttle valve 10 are opened, the second throttle valve 4, the third throttle valve 5, the sixth throttle valve 8, the seventh throttle valve 9 are closed, and the carbon dioxide storage tank 12 supplies CO to the second fixed-bed reactor 2 2 The sensible heat of the generated CO gas is cooled by the first condenser 24 after the reaction with the low-valence metal oxide or the metal simple substance in the multilayer reaction medium 11; the hydrogen storage tank 13 supplies hydrogen to the first fixed bed reactor 1, and reacts with the high valence metal oxide in the multi-layer reaction medium 11 to generate high temperature steam, which is sent to the heat exchange pipeline after heat exchange by the second condenser 25.
Then, low valence metal oxide or metal simple substance in the second fixed bed reaction device 2 is oxidized to generate high valence metal oxide, after the high valence metal oxide in the first fixed bed reaction device 1 is reduced to low valence metal oxide or metal simple substance, the first throttle valve 3, the fourth throttle valve 6, the fifth throttle valve 7 and the eighth throttle valve 10 are closed, the second throttle valve 4, the third throttle valve 5, the sixth throttle valve 8 and the seventh throttle valve 9 are opened, hydrogen in the hydrogen storage tank 13 enters the second fixed bed reaction device 2 and CO in the carbon dioxide storage tank 12 2 The reaction is repeated in the first fixed bed reactor 1.
Thermochemical CO of the invention 2 And CO gas generated by the chemical chain conversion process is used for storage and utilization.
Claims (9)
1. Thermochemical CO 2 An interactive dual fixed bed apparatus for chemical looping conversion comprising CO 2 Chemical looping conversion systems and cyclic thermal systems;
the CO is 2 The chemical chain conversion system comprises a first fixed bed reaction device (1) internally provided with a plurality of layers of reaction media (11) and a second fixed bed reaction device (2) internally provided with a plurality of layers of reaction media (11), wherein the plurality of layers of reaction media (11) are honeycomb-shaped solid oxygen carrier particles;
wherein, the outlet of the carbon dioxide storage tank (12) is communicated with the inlet of the first fixed bed reaction device (1) through a sixth throttling valve (8), and the outlet of the first fixed bed reaction device (1) is communicated with the inlet of the first condenser (24) through a second throttling valve (4); an outlet of the carbon dioxide storage tank (12) is communicated with an inlet of the second fixed bed reaction device (2) through an eighth throttling valve (10), and an outlet of the second fixed bed reaction device (2) is communicated with an inlet of the first condenser (24) through a fourth throttling valve (6);
the outlet of the hydrogen storage tank (13) is communicated with the inlet of the first fixed bed reaction device (1) through a fifth throttling valve (7), and the outlet of the first fixed bed reaction device (1) is communicated with the inlet of the second condenser (25) through a first throttling valve (3); the outlet of the hydrogen storage tank (13) is communicated with the inlet of the second fixed bed reaction device (2) through a seventh throttling valve (9), and the outlet of the second fixed bed reaction device (2) is communicated with the inlet of a second condenser (25) through a third throttling valve (5);
the circulating heat system comprises a first circulating heat exchange system (22), wherein the first circulating heat exchange system (22) comprises a first condenser (24), a second condenser (25), a heat exchanger (26) and a second circulating pump (28) which are communicated through heat exchange pipelines.
2. Thermochemical CO according to claim 1 2 The interactive double-fixed-bed device for chemical chain conversion is characterized in that the circulating heat system further comprises a second circulating heat exchange system (23), and the second circulating heat exchange system (23) comprises a first fixed-bed reaction device (1), a first circulating pump (27), a heat exchanger (26) and a second fixed-bed reaction device (2) which are communicated through heat exchange pipelines.
3. Thermochemical CO according to claim 2 2 The interactive double fixed bed device for chemical chain conversion is characterized in that a first heat exchange medium box (20) is connected with a second circulating heat exchange system (23), and a second heat exchange medium box (21) is connected with a first circulating heat exchange system (22).
4. Thermochemical CO according to claim 2 2 An interactive double fixed bed device for chemical chain conversion is characterized in that the tank bodies of the first fixed bed reaction device (1) and the second fixed bed reaction device (2) are provided with throttle valves for adjustingAnd (4) flow of the heat exchange medium.
5. Thermochemical CO according to claim 1 2 An interactive double fixed bed apparatus for chemical chain conversion is characterized in that a high valence metal oxide is charged into a multi-layer reaction medium (11) in a fixed bed reaction apparatus to which hydrogen is supplied first, and a low valence metal oxide or a simple metal is charged into a multi-layer reaction medium (11) in another fixed bed reaction apparatus.
6. Thermochemical CO treatment by means of an interactive double fixed bed installation according to any of claims 1 to 5 2 Chemical looping conversion process, characterized in that a carbon dioxide storage tank (12) supplies CO to one of the fixed bed reactors 2 The sensible heat of the CO gas generated by the reaction with the lower valence metal oxide or the metal simple substance in the multilayer reaction medium (11) is cooled by a first condenser (24); the hydrogen storage tank (13) supplies hydrogen to the other fixed bed reaction device, reacts with the high valence metal oxide in the multilayer reaction medium (11) to generate high temperature water vapor, and the high temperature water vapor is sent to a heat exchange pipeline after heat exchange through a second condenser (25); after the conversion of the multi-layer reaction medium (11) is finished, the throttle valve is adjusted, and the carbon dioxide storage tank (12) and the hydrogen storage tank (13) are respectively switched to different fixed bed reaction devices to supply CO 2 And hydrogen.
7. Thermochemical CO according to claim 6 2 The chemical looping conversion process is characterized in that a first throttle valve (3), a fourth throttle valve (6), a fifth throttle valve (7) and an eighth throttle valve (10) are opened, a second throttle valve (4), a third throttle valve (5), a sixth throttle valve (8) and a seventh throttle valve (9) are closed, and a carbon dioxide storage tank (12) supplies CO to a second fixed bed reaction device (2) 2 The sensible heat of the CO gas generated by the reaction with the lower valence metal oxide or the metal simple substance in the multilayer reaction medium (11) is cooled by a first condenser (24); the hydrogen storage tank (13) supplies hydrogen to the first fixed bed reactor (1), reacts with the high valence metal oxide in the multi-layer reaction medium (11) to generate high temperature steam, and passes through a second condenser (C)25 After heat exchange, is sent to the heat exchange pipeline.
8. Thermochemical CO according to claim 7 2 The chemical chain conversion process is characterized in that low-valence metal oxide or metal simple substance in the second fixed bed reaction device (2) is oxidized to generate high-valence metal oxide, the high-valence metal oxide in the first fixed bed reaction device (1) is reduced to the low-valence metal oxide or metal simple substance, the first throttle valve (3), the fourth throttle valve (6), the fifth throttle valve (7) and the eighth throttle valve (10) are closed, the second throttle valve (4), the third throttle valve (5), the sixth throttle valve (8) and the seventh throttle valve (9) are opened, hydrogen in the hydrogen storage tank (13) enters the second fixed bed reaction device (2) and CO in the carbon dioxide storage tank (12) 2 Entering a first fixed bed reaction device (1) for repeated reaction.
9. Thermochemical CO according to any of claims 6 2 The chemical chain conversion process is characterized in that the generated CO gas is used for storage and utilization.
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