CN115536553A - Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production - Google Patents
Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production Download PDFInfo
- Publication number
- CN115536553A CN115536553A CN202211144189.2A CN202211144189A CN115536553A CN 115536553 A CN115536553 A CN 115536553A CN 202211144189 A CN202211144189 A CN 202211144189A CN 115536553 A CN115536553 A CN 115536553A
- Authority
- CN
- China
- Prior art keywords
- carbon dioxide
- outlet
- inlet
- storage tank
- hydrogen production
- 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.)
- Pending
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 266
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 133
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 133
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 239000001257 hydrogen Substances 0.000 title claims abstract description 86
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 86
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 72
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 239000003546 flue gas Substances 0.000 title claims abstract description 51
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 34
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 230000009467 reduction Effects 0.000 title claims abstract description 33
- 230000008878 coupling Effects 0.000 title claims abstract description 17
- 238000010168 coupling process Methods 0.000 title claims abstract description 17
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 17
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 92
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 46
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 42
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 42
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 41
- 239000004202 carbamide Substances 0.000 claims abstract description 41
- 238000000926 separation method Methods 0.000 claims abstract description 40
- 238000000746 purification Methods 0.000 claims abstract description 35
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 86
- 238000003860 storage Methods 0.000 claims description 75
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 52
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 41
- 239000001301 oxygen Substances 0.000 claims description 41
- 229910052760 oxygen Inorganic materials 0.000 claims description 41
- 238000010521 absorption reaction Methods 0.000 claims description 24
- 229910052757 nitrogen Inorganic materials 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 21
- 239000006200 vaporizer Substances 0.000 claims description 17
- 239000000779 smoke Substances 0.000 claims description 10
- 239000002808 molecular sieve Substances 0.000 claims description 9
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 8
- 238000011045 prefiltration Methods 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 3
- 229910001873 dinitrogen Inorganic materials 0.000 claims 4
- 239000000126 substance Substances 0.000 abstract description 5
- 238000004134 energy conservation Methods 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 239000003245 coal Substances 0.000 abstract description 2
- 230000018109 developmental process Effects 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 238000002360 preparation method Methods 0.000 description 5
- 239000006096 absorbing agent Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000618 nitrogen fertilizer Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- QOTAEASRCGCJDN-UHFFFAOYSA-N [C].CO Chemical compound [C].CO QOTAEASRCGCJDN-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
- C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
- C07C273/04—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/60—Constructional parts of cells
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Analytical Chemistry (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention belongs to the technical field of energy conservation and emission reduction in coal chemical industry, and particularly relates to a carbon emission reduction system coupling carbon dioxide in flue gas and electrolytic hydrogen production. The carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production comprises a compressor system, a carbon dioxide liquefaction and purification system, a low-temperature air separation system, an ammonia synthesis system, an electrolytic hydrogen production system and a urea synthesis system; the flue gas pipeline is connected with the compressor system; the carbon dioxide liquefaction and purification system is respectively connected with the compressor system, the low-temperature air separation system, the electrolysis hydrogen production system and the urea synthesis system; and the ammonia synthesis system is respectively connected with the electrolytic hydrogen production system, the low-temperature air separation system and the urea synthesis system. The advantages are that: the system has simple structure, not only reduces carbon emission, but also makes full use of new energy, and brings relevant economic and environmental benefits. The system is easy to manufacture, safe and reliable to use and convenient to implement, popularize and apply.
Description
Technical Field
The invention belongs to the technical field of energy conservation and emission reduction in coal chemical industry, and particularly relates to a carbon emission reduction system coupling carbon dioxide in flue gas and electrolytic hydrogen production.
Background
At present, the reduction of carbon emission has great influence on the world ecological environment, and especially in petrochemical and chemical industries, especially nitrogen fertilizer and methanol carbon emission enterprises, the great attention is paid to the world carbon emission reduction situation. CO is introduced into 2 The conversion into chemicals to realize carbon recycling is an important means for reducing carbon emission at the tail end. The urea utilizes CO 2 The traditional chemical products consume 0.75t of carbon dioxide per ton of urea, and the carbon dioxide consumption per year of urea production exceeds 4200 ten thousand t. In addition, the method can be widely adopted, the path dependence of the industry on fossil energy can be thoroughly turned, and the carbon emission reduction pressure of the industry is greatly reduced.
Therefore, the development of the nitrogen fertilizer industry with renewable energy sources is likely to be a long-term development strategy for the industry. In a word, the overall goal of carbon neutralization based on carbon peak-to-peak is determined, the nitrogen fertilizer industry is heavy and arduous, and not only the addition of high-quality development but also the subtraction of carbon emission reduction are needed, so that the carbon emission reduction is driven by innovation, the carbon emission reduction is assisted by energy conservation and consumption reduction, the carbon emission reduction is driven by the high-quality development of the industry, and a greater contribution is made to the realization of the green low-carbon transformation development of the industry.
Based on this, a series of emission reduction systems for carbon dioxide conversion needs to be developed.
Disclosure of Invention
The invention aims to solve the technical problem of providing a carbon emission reduction system which utilizes the coupling of carbon dioxide in flue gas and electrolytic hydrogen production, and effectively overcomes the defects of the prior art.
The technical scheme for solving the technical problems is as follows:
a carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production comprises a compressor system, a carbon dioxide liquefaction and purification system, a low-temperature air separation system, an ammonia synthesis system, an electrolytic hydrogen production system and a urea synthesis system; the flue gas pipeline is connected with the compressor system; the carbon dioxide liquefaction and purification system is respectively connected with the compressor system, the low-temperature air separation system, the electrolysis hydrogen production system and the urea synthesis system; the synthetic ammonia system is respectively connected with the electrolytic hydrogen production system, the low-temperature air separation system and the urea synthesis system; the compressor system is used for compressing flue gas; the carbon dioxide liquefaction and purification system is used for absorbing and purifying carbon dioxide in the flue gas conveyed by the compressor system, respectively conveying the purified carbon dioxide and the produced water to the urea synthesis system and the electrolytic hydrogen production system, and conveying the residual gas of the flue gas to the low-temperature air separation system; the low-temperature air separation system is used for separating oxygen and nitrogen in air entering the low-temperature air separation system and conveying the nitrogen to the synthetic ammonia system; the urea synthesis system is used for preparing and producing urea through the synthetic ammonia and the carbon dioxide conveyed to the urea synthesis system.
On the basis of the technical scheme, the invention can be further improved as follows.
Further, the compressor system comprises a smoke pipeline, a smoke prefilter, a primary compressor and a secondary compressor, wherein the smoke pipeline, the smoke prefilter, the inlet and the outlet of the primary compressor and the inlet and the outlet of the secondary compressor are sequentially connected.
Further, the carbon dioxide liquefaction and purification system comprises a carbon dioxide vaporizer, a condensed water heat exchanger, a cold water heat exchanger at 5 ℃, a steam-water separator, a carbon dioxide absorption tower, a liquid carbon dioxide storage tank, a condensed water storage tank and a carbon dioxide purification tower; the outlet of the secondary compressor, the shell pass inlet and outlet of the carbon dioxide vaporizer, the shell pass inlet and outlet of the condensed water heat exchanger, the shell pass inlet and outlet of the 5 ℃ cold water heat exchanger, the inlet and gas phase outlet of the steam-water separator and the inlet of the carbon dioxide absorption tower are sequentially connected; an outlet of the condensed water storage tank is connected with a tube pass inlet of a condensed water heat exchanger, and a tube pass outlet of the condensed water heat exchanger is connected with the electrolytic hydrogen production system; an inlet of the condensed water storage tank is respectively connected with a liquid phase outlet of the steam-water separator and a bottom outlet of the carbon dioxide purification tower; an outlet of the liquid carbon dioxide storage tank is connected with a tube pass inlet of a carbon dioxide vaporizer, and a tube pass outlet of the carbon dioxide vaporizer is connected with the urea synthesis system; an inlet of the liquid carbon dioxide storage tank is connected with an outlet at the top of the carbon dioxide purification tower; the inlet of the carbon dioxide purifying tower is connected with the outlet at the bottom of the carbon dioxide absorbing tower; the top outlet of the carbon dioxide absorption tower is connected with the low-temperature air separation system.
Further, a tube pass inlet and an outlet of the 5 ℃ cold water heat exchanger are respectively connected with a 5 ℃ circulating cold water waterway.
Further, the low-temperature air separation system comprises a molecular sieve absorber, a low-temperature air separation device, a nitrogen storage tank and an oxygen-enriched air storage tank, wherein the top outlet of the carbon dioxide absorption tower, the inlet and the outlet of the molecular sieve absorber, the inlet and the nitrogen outlet of the low-temperature air separation device and the inlet of the nitrogen storage tank are sequentially connected, the outlet of the nitrogen storage tank is connected with the synthetic ammonia system, and the oxygen outlet of the low-temperature air separation device is connected with the oxygen-enriched air storage tank.
Further, the synthetic ammonia system comprises a synthetic ammonia device, a hydrogen inlet and a nitrogen inlet of the synthetic ammonia device are respectively connected with the electrolytic hydrogen production system and an outlet of the nitrogen storage tank, and a synthetic ammonia outlet of the synthetic ammonia device is connected with the urea synthesis system.
Furthermore, the electrolytic hydrogen production system comprises an electrolytic hydrogen production device, a hydrogen storage tank, an oxygen storage tank and a pure water production device, wherein the tube pass outlet of the condensed water heat exchanger, the inlet and the outlet of the pure water production device and the water quality inlet of the electrolytic hydrogen production device are sequentially connected, the hydrogen outlet of the electrolytic hydrogen production device, the inlet and the outlet of the hydrogen storage tank and the hydrogen inlet of the synthetic ammonia device are sequentially connected, and the oxygen outlet of the electrolytic hydrogen production device is connected with the oxygen storage tank.
Further, the outlet at the top of the carbon dioxide absorption tower is connected with the oxygen-enriched air storage tank.
Further, the oxygen storage tank is connected with a secondary air inlet of the boiler.
The system further comprises a steam turbine, the steam turbine is in transmission connection with the primary compressor, the oxygen-enriched air storage tank is connected with an inlet of the steam turbine, and an outlet of the steam turbine is connected with a secondary air inlet.
The beneficial effects of the invention are: the system has simple structure, not only reduces carbon emission, but also makes full use of new energy, and brings relevant economic and environmental benefits. The system is easy to manufacture, safe and reliable to use, convenient to implement, popularize and apply and has certain practical application prospect.
Drawings
Fig. 1 is a schematic structural diagram of a carbon emission reduction system coupled with hydrogen production by electrolysis using carbon dioxide in flue gas according to the present invention.
In the drawings, the components represented by the respective reference numerals are listed below:
1. a smoke pre-filter; 2. a first stage compressor; 3. a secondary compressor; 4. a carbon dioxide vaporizer; 5. a condensed water heat exchanger; 6. a cold water heat exchanger at 5 ℃; 7. a carbon dioxide purification tower; 8. a condensed water storage tank; 9. a liquid carbon dioxide storage tank; 10. a carbon dioxide absorption tower; 11. a molecular sieve adsorber; 12. a cryogenic air separation plant; 13. a nitrogen storage tank; 14. an ammonia synthesis unit; 15. an oxygen storage tank; 16. a pure water preparation device; 17. an electrolytic hydrogen production device; 18. a hydrogen storage tank; 20. an oxygen-enriched air storage tank; 21. a steam turbine; 30. a steam-water separator.
Detailed Description
The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention.
The embodiment is as follows: as shown in fig. 1, the carbon emission reduction system coupled with hydrogen production by electrolysis using carbon dioxide in flue gas in the embodiment includes a compressor system, a carbon dioxide liquefaction and purification system, a low-temperature air separation system, an ammonia synthesis system, a hydrogen production by electrolysis system, and a urea synthesis system; the flue gas pipeline is connected with the compressor system; the carbon dioxide liquefaction and purification system is respectively connected with the compressor system, the low-temperature air separation system, the electrolysis hydrogen production system and the urea synthesis system; the synthetic ammonia system is respectively connected with the electrolytic hydrogen production system, the low-temperature air separation system and the urea synthesis system;
specifically, in this embodiment, the compressor system is used for compressing flue gas; the carbon dioxide liquefaction and purification system is used for absorbing and purifying carbon dioxide in the flue gas conveyed by the compressor system, respectively conveying the carbon dioxide and the produced water to the urea synthesis system and the electrolytic hydrogen production system after purification, and conveying the residual gas of the flue gas to the low-temperature air separation system; the low-temperature air separation system is used for separating oxygen and nitrogen in air entering the low-temperature air separation system and conveying the nitrogen to the synthetic ammonia system; the urea synthesis system is used for preparing and producing urea through the synthetic ammonia and the carbon dioxide conveyed to the urea synthesis system.
In the whole process, the carbon dioxide in the flue gas is absorbed by a carbon dioxide liquefaction and purification system, the carbon dioxide is purified, the liquid carbon dioxide and water obtained after purification are used as raw materials for preparing urea and for preparing hydrogen by electrolysis, meanwhile, oxygen and nitrogen are separated from the residual gas after the carbon dioxide is absorbed by the flue gas, the hydrogen obtained after the hydrogen is electrolyzed by the hydrogen preparation system and the nitrogen obtained after the flue gas are separated are prepared into synthetic ammonia in a synthetic ammonia system, then, the carbon dioxide and the synthetic ammonia are used as raw materials for preparing the urea in the urea synthesis system, the whole system can fully utilize the carbon dioxide in the flue gas to realize the preparation of the urea, the system is simple in structure, the carbon emission is reduced, new energy is fully utilized, and related economic and environmental benefits are brought. The system is easy to manufacture, safe and reliable to use, convenient to implement, popularize and apply and has certain practical application prospect.
In this embodiment, the structure of each core system is as follows:
a compressor system: including flue gas pipeline, leading filter 1 of flue gas, primary compressor 2 and secondary compressor 3, the import and the export of above-mentioned flue gas pipeline, leading filter 1 of flue gas, primary compressor 2, the import and the export of secondary compressor 3 are connected in order.
Carbon dioxide liquefaction purification system: comprises a carbon dioxide vaporizer 4, a condensed water heat exchanger 5, a cold water heat exchanger 6 with the temperature of 5 ℃, a steam-water separator 30, a carbon dioxide absorption tower 10, a liquid carbon dioxide storage tank 9, a condensed water storage tank 8 and a carbon dioxide purification tower 7; the outlet of the secondary compressor 3, the shell side inlet and outlet of the carbon dioxide vaporizer 4, the shell side inlet and outlet of the condensed water heat exchanger 5, the shell side inlet and outlet of the 5 ℃ cold water heat exchanger 6, the inlet and gas phase outlet of the steam-water separator 30 and the inlet of the carbon dioxide absorption tower 10 are sequentially connected; an outlet of the condensed water storage tank 8 is connected with a tube pass inlet of the condensed water heat exchanger 5, and a tube pass outlet of the condensed water heat exchanger 5 is connected with the electrolytic hydrogen production system; an inlet of the condensed water storage tank 8 is respectively connected with a liquid phase outlet of the steam-water separator 30 and a bottom outlet of the carbon dioxide purification tower 7; the outlet of the liquid carbon dioxide storage tank 9 is connected with the tube pass inlet of the carbon dioxide vaporizer 4, and the tube pass outlet of the carbon dioxide vaporizer 4 is connected with the urea synthesis system; the inlet of the liquid carbon dioxide storage tank 9 is connected with the top outlet of the carbon dioxide purification tower 7; an inlet of the carbon dioxide purifying column 7 is connected to a bottom outlet of the carbon dioxide absorbing column 10; the top outlet of the carbon dioxide absorbing tower 10 is connected to the cryogenic air separation system.
Cryogenic air separation system: the device comprises a molecular sieve absorber 11, a low-temperature air separation device 12, a nitrogen storage tank 13 and an oxygen-enriched air storage tank 20, wherein the top outlet of the carbon dioxide absorption tower 10, the inlet and the outlet of the molecular sieve absorber 11, the inlet and the nitrogen outlet of the low-temperature air separation device 12 and the inlet of the nitrogen storage tank 13 are sequentially connected, the outlet of the nitrogen storage tank 13 is connected with the synthetic ammonia system, and the oxygen outlet of the low-temperature air separation device 12 is connected with the oxygen-enriched air storage tank 20.
A synthetic ammonia system: the device comprises a synthetic ammonia device 14, wherein a hydrogen inlet and a nitrogen inlet of the synthetic ammonia device 14 are respectively connected with outlets of the electrolytic hydrogen production system and the nitrogen storage tank 13, and a synthetic ammonia outlet of the synthetic ammonia device 14 is connected with the urea synthesis system.
An electrolytic hydrogen production system: the system comprises an electrolytic hydrogen production device 17, a hydrogen storage tank 18, an oxygen storage tank 15 and a pure water production device 16, wherein a tube pass outlet of the condensed water heat exchanger 5, an inlet and an outlet of the pure water production device 16 and a water quality inlet of the electrolytic hydrogen production device 17 are sequentially connected, a hydrogen outlet of the electrolytic hydrogen production device 17, an inlet and an outlet of the hydrogen storage tank 18 and a hydrogen inlet of the synthetic ammonia device 14 are sequentially connected, and an oxygen outlet of the electrolytic hydrogen production device 17 is connected with the oxygen storage tank 15.
The whole system is used by a power plant as an example, flue gas in a boiler of a power plant area is used as a source of carbon dioxide, and the operation specific process is as follows:
1) Introducing the filtered boiler flue gas into a flue gas pipeline, and starting a secondary compressor 3 to gradually increase the pressure;
2) Starting a 5 ℃ cold water heat exchanger 6, controlling the air quantity of a secondary compressor 3 to ensure that the temperature of the flue gas is reduced to 5-10 ℃, introducing the flue gas into a steam-water separator 30, introducing a gas phase into a carbon dioxide absorption tower 10, and introducing a liquid phase into a condensed water storage tank 8;
3) The air coming out of the top of the carbon dioxide absorption tower 10 directly enters an oxygen-enriched air storage tank 20 (in the embodiment, the outlet at the top of the carbon dioxide absorption tower 10 is connected with the oxygen-enriched air storage tank 20), the pressure is adjusted, a primary compressor 2 is started, and the smoke pressure is further increased to 4-5MPa;
4) When the liquid level at the bottom of the carbon dioxide absorption tower 10 is enough, starting an absorption tower circulating pump on a pipeline connected with the carbon dioxide purification tower 7 at the bottom of the carbon dioxide absorption tower 10, when the liquid level is continuously raised, starting an outlet valve at the bottom of the carbon dioxide absorption tower 10, controlling the opening of a valve of the outlet valve to send liquid into the carbon dioxide purification tower 7, when the carbon dioxide purification tower 7 is full of liquid level, adjusting the valve at the top of the carbon dioxide purification tower 7 to send liquid carbon dioxide into a liquid carbon dioxide storage tank 9, and adjusting a valve at the bottom of the carbon dioxide purification tower 7 to send water into a condensed water storage tank 8;
5) When the condensed water storage tank 8 is at a high liquid level, a conveying pump on a pipeline between an outlet of the condensed water storage tank 8 and a shell pass inlet of the condensed water heat exchanger 5 is started, condensed water is sent into the condensed water heat exchanger 5 to exchange heat with flue gas passing through the shell pass of the condensed water heat exchanger 5, the temperature of the flue gas is reduced, and meanwhile, liquid carbon dioxide in the liquid carbon dioxide storage tank 9 is sent into the carbon dioxide vaporizer 4 to exchange heat with the flue gas passing through the shell pass of the carbon dioxide vaporizer 4, so that the temperature of the flue gas is reduced;
6) When the concentration of carbon dioxide at the outlet of the carbon dioxide absorption tower 10 is reduced to be below 400ppm, introducing the carbon dioxide into a molecular sieve adsorber 11 and a low-temperature air separation device 12, when the low-temperature air separation device 12 operates normally, sending qualified nitrogen to an ammonia synthesis device 14, and sending separated oxygen into an oxygen-enriched air storage tank 20;
7) And starting the pure water preparation device 16, preparing the condensed water subjected to heat exchange with the flue gas into pure water, sending the pure water into the electrolytic hydrogen preparation device 17, and sending qualified hydrogen into the synthetic ammonia device 14 through the hydrogen storage tank 18.
8) The ammonia synthesis device 14 sends the synthesis ammonia to the urea synthesis system, and the synthesis ammonia and the carbon dioxide coming from the carbon dioxide vaporizer 4 are used as raw materials to finally prepare the output urea.
In a preferred embodiment, the oxygen storage tank 15 is connected to a overfire air inlet of the boiler.
In the above embodiment, the oxygen generated by the electrolytic hydrogen production device 17 is introduced into the secondary air port of the boiler and participates in the combustion operation process inside the boiler as the secondary air, so that the energy consumption is reduced to a certain extent, and the effects of energy conservation and emission reduction are achieved.
In the embodiment, the energy-saving and emission-reducing boiler further comprises a steam turbine 21, the steam turbine 21 is in transmission connection with the primary compressor 2, the steam turbine 21 drives the primary compressor 2 to operate, the oxygen-enriched air storage tank 20 is connected with an inlet of the steam turbine 21, an outlet of the steam turbine 21 is connected with a secondary air inlet, high-pressure oxygen-enriched air serves as a kinetic energy source of the steam turbine 21, the oxygen-enriched air storage tank 20 can serve as an adsorption tower regeneration air source, the air absorbs heat and then works at the steam turbine 21, the effects of energy saving and emission reduction are fully achieved, meanwhile, air after working enters the boiler again and participates in the combustion operation process inside the boiler as secondary air, and energy saving and emission reduction are achieved.
In this embodiment, in the process 1), after the secondary compressor 3 is started, the line between the oxygen-enriched air storage tank 20 and the turbine 21 is opened, so that the primary compressor 2 starts operating step by step.
In this embodiment, the communication between each structure or device is implemented by pipeline communication, and valves are flexibly and reasonably arranged on each pipeline according to actual use requirements, so as to achieve the purpose of adjusting the flow rate of the fluid in the pipeline.
In the embodiment, the flue gas prefilter 1, the carbon dioxide vaporizer 4, the condensed water heat exchanger 5, the 5 ℃ cold water heat exchanger 6, the steam-water separator 30, the carbon dioxide absorption tower 10, the liquid carbon dioxide storage tank 9, the carbon dioxide purification tower 7, the molecular sieve adsorber 11, the low-temperature air separation plant 12, the ammonia synthesis plant 14, the electrolytic hydrogen production plant 17 and the pure water production plant 16 are all conventional devices in the field, and the specific models can be flexibly and reasonably selected according to actual use requirements, or simple parameter adjustment is performed on the basis of the conventional devices, particularly, the 5 ℃ cold water heat exchanger 6 is a conventional cold water heat exchanger, but the heat exchange is performed by using 5 ℃ cold water, wherein the electrolytic hydrogen production plant 17 can adopt existing photovoltaic electrolytic hydrogen production equipment on the market, solar energy is fully utilized, and the energy-saving and emission-reducing effects are better. Others are not described in detail herein.
In this example, the urea synthesis system uses a urea synthesis tower (indicated by a in the figure) of the prior art.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of the invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless explicitly specified otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be interconnected within two elements or in a relationship where two elements interact with each other unless otherwise specifically limited. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature "under," "beneath," and "under" a second feature may be directly under or obliquely under the second feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (10)
1. A carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production is characterized in that: comprises a compressor system, a carbon dioxide liquefaction and purification system, a low-temperature air separation system, an ammonia synthesis system, an electrolytic hydrogen production system and a urea synthesis system; the flue gas pipeline is connected with the compressor system; the carbon dioxide liquefaction and purification system is respectively connected with the compressor system, the low-temperature air separation system, the electrolysis hydrogen production system and the urea synthesis system; the synthetic ammonia system is respectively connected with the electrolytic hydrogen production system, the low-temperature air separation system and the urea synthesis system; the compressor system is used for compressing flue gas; the carbon dioxide liquefaction and purification system is used for absorbing and purifying carbon dioxide in the flue gas conveyed by the compressor system, respectively conveying the carbon dioxide and the produced water to the urea synthesis system and the electrolytic hydrogen production system after purification, and conveying the residual gas of the flue gas to the low-temperature air separation system; the electrolytic hydrogen production system is used for absorbing water quality, preparing pure water, electrolyzing the pure water to produce hydrogen and oxygen, and conveying the produced hydrogen to the synthetic ammonia system, and the low-temperature air separation system is used for separating oxygen and nitrogen in air entering the low-temperature air separation system and conveying the nitrogen to the synthetic ammonia system; the urea synthesis system is used for preparing and producing urea through the synthetic ammonia and the carbon dioxide conveyed to the urea synthesis system.
2. The carbon emission reduction system coupling the production of hydrogen by carbon dioxide in flue gas and electrolysis according to claim 1, wherein: the compressor system comprises a smoke pipeline, a smoke prefilter (1), a primary compressor (2) and a secondary compressor (3), wherein the smoke pipeline, the smoke prefilter (1), the inlet and the outlet of the primary compressor (2) and the inlet and the outlet of the secondary compressor (3) are sequentially connected.
3. The carbon emission reduction system coupling the production of hydrogen by carbon dioxide in flue gas and electrolysis according to claim 2, wherein: the carbon dioxide liquefaction and purification system comprises a carbon dioxide vaporizer (4), a condensed water heat exchanger (5), a cold water heat exchanger (6) at 5 ℃, a steam-water separator (30), a carbon dioxide absorption tower (10), a liquid carbon dioxide storage tank (9), a condensed water storage tank (8) and a carbon dioxide purification tower (7);
an outlet of the secondary compressor (3), a shell pass inlet and an outlet of the carbon dioxide vaporizer (4), a shell pass inlet and an outlet of the condensed water heat exchanger (5), a shell pass inlet and an outlet of the 5 ℃ cold water heat exchanger (6), an inlet and a gas phase outlet of the steam-water separator (30) and an inlet of the carbon dioxide absorption tower (10) are sequentially connected;
an outlet of the condensed water storage tank (8) is connected with a tube pass inlet of the condensed water heat exchanger (5), and a tube pass outlet of the condensed water heat exchanger (5) is connected with the electrolytic hydrogen production system;
an inlet of the condensed water storage tank (8) is respectively connected with a liquid phase outlet of the steam-water separator (30) and a bottom outlet of the carbon dioxide purification tower (7);
an outlet of the liquid carbon dioxide storage tank (9) is connected with a tube pass inlet of the carbon dioxide vaporizer (4), and a tube pass outlet of the carbon dioxide vaporizer (4) is connected with the urea synthesis system;
an inlet of the liquid carbon dioxide storage tank (9) is connected with an outlet at the top of the carbon dioxide purification tower (7);
the inlet of the carbon dioxide purification tower (7) is connected with the bottom outlet of the carbon dioxide absorption tower (10);
the top outlet of the carbon dioxide absorption tower (10) is connected with the low-temperature air separation system.
4. The carbon emission reduction system using coupling of carbon dioxide in flue gas and hydrogen production by electrolysis according to claim 3, wherein: and the tube pass inlet and the tube pass outlet of the 5 ℃ cold water heat exchanger (6) are respectively connected with a 5 ℃ circulating cold water waterway.
5. The carbon emission reduction system coupling the production of hydrogen by carbon dioxide in flue gas and electrolysis according to claim 3, wherein: the low temperature air separation system includes molecular sieve adsorber (11), low temperature air separation plant (12), nitrogen gas storage tank (13) and oxygen enriched air storage tank (20), the import and the export of the top export of carbon dioxide absorption tower (10), molecular sieve adsorber (11), the entry and the nitrogen gas export of low temperature air separation plant (12), the import of nitrogen gas storage tank (13) are connected in order, the export of nitrogen gas storage tank (13) with synthetic ammonia headtotail, the oxygen outlet connection of low temperature air separation plant (12) oxygen enriched air storage tank (20).
6. The carbon emission reduction system using coupling of carbon dioxide in flue gas and hydrogen production by electrolysis according to claim 5, wherein: the synthetic ammonia system comprises a synthetic ammonia device (14), a hydrogen inlet and a nitrogen inlet of the synthetic ammonia device (14) are respectively connected with the electrolytic hydrogen production system and an outlet of the nitrogen storage tank (13), and a synthetic ammonia outlet of the synthetic ammonia device (14) is connected with the urea synthesis system.
7. The carbon emission reduction system using coupling of carbon dioxide in flue gas and hydrogen production by electrolysis according to claim 6, wherein: the electrolytic hydrogen production system comprises an electrolytic hydrogen production device (17), a hydrogen storage tank (18), an oxygen storage tank (15) and a pure water production device (16), wherein the tube pass outlet of the condensed water heat exchanger (5), the inlet and outlet of the pure water production device (16) and the water inlet of the electrolytic hydrogen production device (17) are sequentially connected, the hydrogen outlet of the electrolytic hydrogen production device (17), the inlet and outlet of the hydrogen storage tank (18) and the hydrogen inlet of the synthetic ammonia device (14) are sequentially connected, and the oxygen outlet of the electrolytic hydrogen production device (17) is connected with the oxygen storage tank (15).
8. The carbon emission reduction system coupling the production of hydrogen by carbon dioxide in flue gas and electrolysis according to claim 7, wherein: the top outlet of the carbon dioxide absorption tower (10) is connected with the oxygen-enriched air storage tank (20).
9. The carbon emission reduction system using coupling of carbon dioxide in flue gas and hydrogen production by electrolysis according to claim 8, wherein: the oxygen storage tank (15) is connected with a secondary air inlet of the boiler.
10. The carbon emission reduction system coupling the production of hydrogen by carbon dioxide in flue gas and electrolysis according to claim 8 or 9, wherein: the system is characterized by further comprising a steam turbine (21), wherein the steam turbine (21) is in transmission connection with the primary compressor (2), the oxygen-enriched air storage tank (20) is connected with an inlet of the steam turbine (21), and an outlet of the steam turbine (21) is connected with a secondary air inlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211144189.2A CN115536553A (en) | 2022-09-20 | 2022-09-20 | Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211144189.2A CN115536553A (en) | 2022-09-20 | 2022-09-20 | Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115536553A true CN115536553A (en) | 2022-12-30 |
Family
ID=84727000
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211144189.2A Pending CN115536553A (en) | 2022-09-20 | 2022-09-20 | Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115536553A (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130288143A1 (en) * | 2012-04-27 | 2013-10-31 | Xfc Inc | Fuel cell using seawater electrolyzer, methods for producing caustic soda, ammonia, urea and pvc using the seawater electrolyzer and integrated system thereof |
| CN108729965A (en) * | 2018-06-08 | 2018-11-02 | 华南理工大学 | The electricity generation system and CO of the part oxygen-enriched combusting of Combined with Calcium base chain2Capture method |
| CN109232161A (en) * | 2018-11-15 | 2019-01-18 | 中国华能集团清洁能源技术研究院有限公司 | In a kind of power-plant flue gas carbon dioxide recovery with utilize system and method |
| CN111378980A (en) * | 2020-04-27 | 2020-07-07 | 中国华能集团清洁能源技术研究院有限公司 | Energy storage system and method for coproducing hydrogen and urea |
| US20200291901A1 (en) * | 2017-11-29 | 2020-09-17 | Weining Song | Total recycling system of capturing, conversion and utilization of flue gas from factory, power plant and refinery |
| CN211999936U (en) * | 2020-04-27 | 2020-11-24 | 中国华能集团清洁能源技术研究院有限公司 | Energy storage system for coproduction of hydrogen and urea |
| CN113307288A (en) * | 2021-04-08 | 2021-08-27 | 中国大唐集团科学技术研究院有限公司火力发电技术研究院 | System and method for efficiently and cleanly synthesizing ammonia/urea by relying on thermal power plant |
| CN218435560U (en) * | 2022-09-20 | 2023-02-03 | 北京清新环境技术股份有限公司 | Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production |
-
2022
- 2022-09-20 CN CN202211144189.2A patent/CN115536553A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130288143A1 (en) * | 2012-04-27 | 2013-10-31 | Xfc Inc | Fuel cell using seawater electrolyzer, methods for producing caustic soda, ammonia, urea and pvc using the seawater electrolyzer and integrated system thereof |
| US20200291901A1 (en) * | 2017-11-29 | 2020-09-17 | Weining Song | Total recycling system of capturing, conversion and utilization of flue gas from factory, power plant and refinery |
| CN108729965A (en) * | 2018-06-08 | 2018-11-02 | 华南理工大学 | The electricity generation system and CO of the part oxygen-enriched combusting of Combined with Calcium base chain2Capture method |
| CN109232161A (en) * | 2018-11-15 | 2019-01-18 | 中国华能集团清洁能源技术研究院有限公司 | In a kind of power-plant flue gas carbon dioxide recovery with utilize system and method |
| CN111378980A (en) * | 2020-04-27 | 2020-07-07 | 中国华能集团清洁能源技术研究院有限公司 | Energy storage system and method for coproducing hydrogen and urea |
| CN211999936U (en) * | 2020-04-27 | 2020-11-24 | 中国华能集团清洁能源技术研究院有限公司 | Energy storage system for coproduction of hydrogen and urea |
| CN113307288A (en) * | 2021-04-08 | 2021-08-27 | 中国大唐集团科学技术研究院有限公司火力发电技术研究院 | System and method for efficiently and cleanly synthesizing ammonia/urea by relying on thermal power plant |
| CN218435560U (en) * | 2022-09-20 | 2023-02-03 | 北京清新环境技术股份有限公司 | Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20200381757A1 (en) | Hydrated magnesium hydride energy system | |
| US20170183226A1 (en) | Residual gas heat exchange combustion-supporting system based on methanol-water mixture reforming hydrogen production system, and method thereof | |
| CN113350989A (en) | Carbon dioxide capture method and system for coal-fired power generation coupled with renewable energy power generation | |
| CN208735278U (en) | Hydrogen conveying system | |
| CN106914117B (en) | Device suitable for continuously capturing carbon dioxide in cement kiln flue gas and generating electricity | |
| CN114214637B (en) | Device and method for comprehensively utilizing hydrogen and oxygen by water electrolysis | |
| CN113479906A (en) | Renewable energy source ammonia synthesis system combining cooling, heating and power | |
| CN105115245A (en) | System device for trapping liquefied carbon dioxide by using cold energy of liquefied natural gas and method of device | |
| CN111748366A (en) | Device and method for directly preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation | |
| CN218435560U (en) | Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production | |
| CN113526525A (en) | Synthetic ammonia tower and renewable energy source synthetic ammonia system with waste heat step recovery | |
| CN106837439A (en) | The vacuum pressure and temperature varying Coupling Adsorption carbon trapping system of solar energy organic Rankine bottoming cycle auxiliary | |
| CN205973803U (en) | Low pressure waste boiler for nitric acid device | |
| CN114349195B (en) | Marine seawater desalination system taking carbon dioxide recovery into consideration and working method | |
| CN212246906U (en) | Device for directly preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation | |
| CN210635950U (en) | Biogas preparation device combining biogas purification and carbon dioxide methanation | |
| CN115536553A (en) | Carbon emission reduction system utilizing coupling of carbon dioxide in flue gas and electrolytic hydrogen production | |
| CN219429725U (en) | Coupling system for household garbage incineration power plant and hydro-ammonia alcohol preparation | |
| CN218811464U (en) | Utilizing CO in flue gas 2 Carbon emission reduction system for synthesizing methanol by solar electrolytic hydrogen production | |
| CN216320988U (en) | Carbon dioxide pressurization recycling device of combined alkali preparation process | |
| CN113479905B (en) | Self-deoxidization ammonia synthesis tower and renewable energy source ammonia synthesis system | |
| CN211998808U (en) | Hydrogen separation and water gas reforming integrated ultrahigh pressure hydrogen production system | |
| CN114522518A (en) | Carbon-containing recycling gas power plant low-cost carbon emission reduction system and method | |
| CN111849574A (en) | Device and method for storing and transporting natural gas based on hydrate method | |
| CN205549977U (en) | Carbon dioxide capture system is jointly assisted with geothermal energy to solar energy |
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 |