CN219156784U - Device for replacing coal by ammonia hydrogen supply in cement clinker production line - Google Patents
Device for replacing coal by ammonia hydrogen supply in cement clinker production line Download PDFInfo
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- CN219156784U CN219156784U CN202320248380.5U CN202320248380U CN219156784U CN 219156784 U CN219156784 U CN 219156784U CN 202320248380 U CN202320248380 U CN 202320248380U CN 219156784 U CN219156784 U CN 219156784U
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 315
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 122
- 239000001257 hydrogen Substances 0.000 title claims abstract description 93
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 93
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 83
- 239000004568 cement Substances 0.000 title claims abstract description 54
- 239000003245 coal Substances 0.000 title claims abstract description 50
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 49
- 238000005336 cracking Methods 0.000 claims abstract description 33
- 238000002309 gasification Methods 0.000 claims abstract description 31
- 238000001354 calcination Methods 0.000 claims abstract description 21
- 238000003860 storage Methods 0.000 claims abstract description 20
- 230000007246 mechanism Effects 0.000 claims abstract description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 41
- 239000003546 flue gas Substances 0.000 claims description 41
- 238000000197 pyrolysis Methods 0.000 claims description 29
- 239000002994 raw material Substances 0.000 claims description 12
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 36
- 229910052799 carbon Inorganic materials 0.000 abstract description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 20
- 238000002485 combustion reaction Methods 0.000 abstract description 19
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- 235000012054 meals Nutrition 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000003345 natural gas Substances 0.000 description 5
- 239000000779 smoke Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000003723 Smelting Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
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- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical group [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
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Abstract
An ammonia hydrogen supply coal replacing device in a cement clinker production line belongs to the technical field of hydrogen energy carbon reduction. The device comprises a cement clinker production line, a liquid ammonia storage tank (5), a liquid ammonia gasification device and an ammonia cracking device, wherein the liquid ammonia storage tank (5) is connected with a liquid ammonia gasification mechanism, the liquid ammonia gasification mechanism is connected with the ammonia cracking device, and the ammonia cracking device is connected to a combustor in the cement clinker production line through a hydrogen supply pipeline (14). Compared with the storage and transportation of liquid hydrogen, the method for storing the liquid ammonia by adopting the liquid ammonia is safer and more convenient, the method is used for gasifying and cracking the liquid ammonia to supply hydrogen by recycling the heat on the production line nearby, and the hydrogen is mixed into the combustor of the cement clinker production line for combustion, so that the coal and the carbon can be greatly reduced, and the low-carbon green development of the cement industry is effectively driven. In addition, when ammonia is cracked, part of cracked ammonia enters the burner along with hydrogen, and the ammonia has the effects of removing nitrogen oxides and inhibiting the generation of nitrogen oxides, so that the nitrogen oxides generated by calcination can be effectively reduced, and the ultra-low emission standard is met.
Description
Technical Field
An ammonia hydrogen supply coal replacing device in a cement clinker production line belongs to the technical field of hydrogen energy carbon reduction.
Background
China is the largest cement production country worldwide, the cement yield still has a rising trend, and along with the rising cement yield, the carbon emission of the cement industry also rises year by year, and reaches the highest historical value of 13.84 hundred million tons in 2020. According to the paris agreement in 2015, the global cement industry must achieve the goal of carbon neutralization in 2050 and 40% carbon reduction in 2030, which has an important impact on the cement production industry in terms of carbon reduction work.
35% of the carbon emissions in cement production come from coal, 60% of which are in the decomposing furnace and 40% of which are in the calcining kiln, and hydrogen energy sources can provide carbon-free alternative fuels on a large scale, stably and reliably through industrial means. The main mode at present is to adopt the scheme of replacing coal by hydrogen-doped natural gas, but the problem of inconvenient large-scale storage and transportation of hydrogen exists, and the problem of unstable combustion caused by directly doping hydrogen into natural gas is solved, so that the technical problem of the combustion stability of the hydrogen-doped natural gas still cannot be thoroughly solved at present.
Disclosure of Invention
The utility model aims to solve the technical problems that: the device for replacing coal with ammonia and hydrogen in the cement clinker production line is provided, the liquid ammonia is easy to store, and the heat on the clinker line can be utilized to heat, gasify and crack the liquid ammonia for hydrogen supply, and the hydrogen directly enters a kiln for combustion, so that the combustion stability is good.
The technical scheme adopted for solving the technical problems is as follows: the device for replacing coal by ammonia and hydrogen in the cement clinker production line is characterized in that: the device comprises a cement clinker production line, a liquid ammonia storage tank, a liquid ammonia gasification device and an ammonia cracking device, wherein the liquid ammonia storage tank is connected with the liquid ammonia gasification mechanism, the liquid ammonia gasification mechanism is connected with the ammonia cracking device, and the ammonia cracking device is connected to a combustor in the cement clinker production line through a hydrogen supply pipeline.
Preferably, the burner comprises a decomposing furnace hydrogen burner and a rotary kiln hydrogen burner, wherein the decomposing furnace hydrogen burner is arranged on a decomposing furnace of the cement clinker production line, and the rotary kiln hydrogen burner is arranged on a rotary kiln of the cement clinker production line.
Preferably, a plurality of decomposing furnace hydrogen burners are arranged in both the horizontal direction and the vertical direction of the decomposing furnace.
Preferably, a plurality of rotary kiln hydrogen burners are axially arranged on the rotary kiln.
The liquid ammonia gasification device and the ammonia cracking device nearly recycle the heat of different grades on the clinker line to gasify and crack the liquid ammonia for hydrogen supply, so that the technical route of replacing coal with the hydrogen supply of the ammonia is easier to popularize. The project recycles the medium-low temperature waste heat of the calcination working section and is used for evaporating liquid ammonia and preheating ammonia; and then the ammonia gas is cracked by recycling high-temperature heat, so that the comprehensive utilization efficiency of the heat is greatly improved.
Preferably, the liquid ammonia gasification device comprises a gasification tank and a liquid ammonia heater, wherein a calcination heat exchanger is arranged on the outer wall of a decomposing furnace and/or a rotary kiln of the cement clinker production line, and the calcination heat exchanger is connected with the liquid ammonia heater through a heat exchange pipeline.
Preferably, an ammonia buffer tank is further arranged between the liquid ammonia gasification device and the ammonia cracking device.
Preferably, an ammonia preheater is arranged on the inner side or the outer side of the ammonia buffer tank, and the ammonia preheater is connected with the calcination heat exchanger.
Preferably, the ammonia cracking device comprises an ammonia cracking tank and an ammonia cracking heater, wherein the ammonia cracking heater is arranged on the inner side or the outer side of the ammonia cracking tank, and the ammonia cracking heater is communicated with a flue gas outlet of a decomposing furnace of the cement clinker production line.
Preferably, the flue gas outlet of the decomposing furnace is connected with a plurality of raw material preheaters, the heat exchange flue gas outlet of the raw material preheaters is connected with a flue gas collecting pipe, and the inlet of the ammonia pyrolysis heater is connected with the flue gas collecting pipe.
Preferably, the flue gas collecting pipe is connected with the flue gas denitration treatment device through an outlet of the ammonia pyrolysis heater.
Compared with the prior art, the technical scheme of the device for replacing coal by ammonia and hydrogen in the cement clinker production line has the beneficial effects that:
1. the utility model stores hydrogen in liquid ammonia, the volume of the liquid ammonia is smaller, and the liquid ammonia has a mature large-scale storage and transportation system, compared with the storage and transportation liquid hydrogen, the liquid ammonia is safer and more convenient. The ammonia cracking hydrogen is mixed into a combustor of a cement clinker production line for combustion, so that partial coal is replaced, coal reduction and carbon reduction can be greatly realized, carbon trade income is obtained, and the low-carbon green development of the cement industry is effectively driven.
In addition, ammonia is limited by thermodynamic equilibrium limit during cracking, part of uncracked ammonia enters a combustor along with hydrogen during ammonia cracking, and ammonia has the effects of removing nitrogen oxides and inhibiting the generation of nitrogen oxides, so that nitrogen oxides generated by calcining in a decomposing furnace and a rotary kiln can be reduced.
2. The device is provided with a plurality of decomposing furnace hydrogen burners in the horizontal direction and the vertical direction of the decomposing furnace, and a plurality of rotary kiln hydrogen burners are arranged in the axial direction of the rotary kiln, so that the device can realize the similarity with a temperature field and a flow field before hydrogen-doped combustion, and the positions of the hydrogen burners are deeply optimized, so that the product quality of clinker can be further improved.
3. The liquid ammonia gasification device and the ammonia cracking device can recover and utilize heat of different grades on a clinker production line nearby to gasify and crack the liquid ammonia for hydrogen supply, so that the comprehensive utilization efficiency of the heat is greatly improved, and the technical route of replacing coal with the ammonia for hydrogen supply is easier to popularize.
Drawings
FIG. 1 is a schematic diagram of an apparatus for replacing coal with ammonia in a cement clinker production line.
Wherein: 1. decomposing furnace 2, rotary kiln 3, raw material preheater 4, flue gas collecting pipe 5, liquid ammonia storage tank 6, gasification tank 7, ammonia cracking tank 8, liquid ammonia heater 9, ammonia cracking heater 10, flue gas denitration treatment device 11, ammonia buffer tank 12, ammonia preheater 13, calcining heat exchanger 14, hydrogen supply pipeline 101, decomposing furnace coal burner 102, decomposing furnace hydrogen burner 201, rotary kiln coal burner 202, and rotary kiln hydrogen burner.
Detailed Description
FIG. 1 is a preferred embodiment of the apparatus for replacing coal with ammonia in a cement clinker production line, and the present utility model will be further described with reference to FIG. 1.
Referring to fig. 1, the cement clinker production line mainly comprises a decomposing furnace 1 and a rotary kiln 2, wherein a smoke outlet of the decomposing furnace 1 is connected with a plurality of raw material preheaters 3, a heat exchange smoke outlet of each raw material preheater 3 is connected with a smoke collecting pipe 4, and the smoke collecting pipe 4 is connected with a smoke denitration treatment device 10. Raw meal firstly passes through a raw meal preheater 3, is preheated by high-temperature flue gas generated by a decomposing furnace 1 and then enters the decomposing furnace 1, a decomposing furnace coal burner 101 is arranged at the lower end of the decomposing furnace 1, a rotary kiln coal burner 201 is arranged at one end of a rotary kiln 2, the raw meal is calcined in the decomposing furnace 1, and the calcined raw meal in the decomposing furnace 1 enters the rotary kiln 2 to be calcined to become clinker. The flue gas collection pipe 4 sends the flue gas into the flue gas denitration treatment device 10 for denitration treatment.
The device for replacing coal by ammonia and hydrogen in the cement clinker production line comprises a liquid ammonia storage tank 5, a liquid ammonia gasification device and an ammonia cracking device, wherein the liquid ammonia storage tank 5 is connected with a liquid ammonia gasification mechanism, the liquid ammonia gasification mechanism is connected with the ammonia cracking device, the ammonia cracking device is connected to a decomposing furnace 1 and a rotary kiln 2 in the cement clinker production line through a hydrogen supply pipeline 14, and the decomposing furnace 1 and the rotary kiln 2 are provided with hydrogen burners, so that 'ammonia' without carbon is used as fuel to replace coal in cement clinker production, and CO2 emission is reduced. The combustion reaction temperature in the decomposing furnace 1 and the rotary kiln 2 can be stabilized by gradually increasing the inlet amount of ammonia pyrolysis gas and gradually reducing the input amount of coal dust during combustion, so that the substitution effect of substituting a certain amount of coal with liquid ammonia is achieved.
The hydrogen-substituted coal is not completely substituted, the coal is still the main coal at present, and in the preliminary test stage, 5% of the total carbon quantity is substituted at present, namely 5% of carbon reduction is realized, and the subsequent hope is that 20% or more can be gradually substituted. The hydrogen amount of the liquid ammonia with the same volume is 60% more than that of the liquid hydrogen, so the volume of the liquid ammonia is smaller due to the hydrogen with the same mass, and the liquid ammonia has a mature large-scale storage and transportation system, so that the liquid ammonia is safer and more convenient compared with the storage and transportation of the liquid hydrogen. Therefore, the utility model directly uses the hydrogen generated after the gasification and the pyrolysis of the liquid ammonia in the liquid ammonia storage tank 5 to replace part of coal for combustion.
In the present embodiment, a plurality of decomposing furnace hydrogen burners 102 are arranged in both the horizontal direction and the vertical direction of the decomposing furnace 1, and the decomposing furnace hydrogen burners 102 are connected to the hydrogen supply pipe 14. A plurality of rotary kiln hydrogen burners 202 are arranged in the axial direction and the radial direction of the rotary kiln 2, and the rotary kiln hydrogen burners 202 are connected to the hydrogen supply line 14. This is so arranged because, in contrast to the combustion of coal, the ignition energy barrier of hydrogen is lower than that of coal, the flame propagation speed is faster than that of coal, the heat release rate is higher than that of coal, and the tail gas composition is mainly gaseous water, which results in the possibility that the temperature distribution in the axial and radial directions in the decomposing furnace 1 and the rotary kiln 2 after the loading combustion is different from that before the loading, thereby affecting the product quality of the clinker. Therefore, in this embodiment, a plurality of hydrogen burners are disposed in the axial direction and the radial direction of the decomposing furnace 1 and the rotary kiln 2, respectively, so that the temperature field and the flow field are similar to those before hydrogen-doped combustion, and the positions of the hydrogen burners are deeply optimized, so that the product quality of clinker can be further improved. The burner interfaces are reserved on the decomposing furnace 1 and the rotary kiln 2, so that the subsequent upgrading to larger blending burning proportion is facilitated, and the emission of nitrogen oxides in tail gas after blending burning does not exceed the upper emission limit specified by the current environmental protection department.
In order to ensure the stability technology of the temperature field and the flow field during the mixed combustion of hydrogen and coal, the temperature and flow velocity distribution of a plurality of positions in the axial direction and the radial direction of the decomposing furnace 1 and the rotary kiln 2 before and after the hydrogen addition needs to be monitored in real time, and the three-dimensional conformation of the temperature and the flow velocity is drawn by combining computational fluid mechanics and heat transfer simulation software. Wherein the temperature is measured by a thermocouple, and the flow rate is measured by a method of tracking the axial ammonia concentration.
The liquid ammonia gasification device and the ammonia cracking device can recover and utilize heat of different grades on a clinker production line nearby to gasify and crack the liquid ammonia for hydrogen supply, so that the comprehensive utilization efficiency of the heat is greatly improved, and the technical route of replacing coal with the ammonia for hydrogen supply is easier to popularize.
Specifically, the liquid ammonia gasification device comprises a gasification tank 6 and a liquid ammonia heater 8, liquid ammonia in a liquid ammonia storage tank 5 enters the gasification tank 6 through a pipeline with a one-way valve, the liquid ammonia heater 8 is a liquid ammonia heating pipe which is arranged on the outer wall of the gasification tank 6 in a surrounding mode, a calcining heat exchanger 13 is arranged on the outer walls of a decomposing furnace 1 and a rotary kiln 2 of a cement clinker production line, the calcining heat exchanger 13 is connected with the liquid ammonia heating pipe through a heat exchange pipeline, the calcining heat exchanger 13 is used for recovering heat generated by calcining the decomposing furnace 1 and the rotary kiln 2, and then water is used as a medium, and the liquid ammonia in the gasification tank 6 is heated through the liquid ammonia heater 8 to gasify the liquid ammonia.
The ammonia pyrolysis device comprises an ammonia pyrolysis tank 7 and an ammonia pyrolysis heater 9, the ammonia pyrolysis heater 9 is a coil pipe arranged on the inner side or the outer side of the ammonia pyrolysis tank 7, a flue gas outlet of the decomposing furnace 1 is connected with a plurality of raw material preheaters 3, a heat exchange flue gas outlet of each raw material preheater 3 is connected with a flue gas collecting pipe 4, an inlet of the ammonia pyrolysis heater 9 is connected with the flue gas collecting pipe 4, a part of flue gas after raw materials are preheated in the flue gas collecting pipe 4 enters the ammonia pyrolysis heater 9, ammonia in the ammonia pyrolysis tank 7 is heated to be cracked into hydrogen and nitrogen, the flue gas collecting pipe 4 is connected with a flue gas denitration treatment device 10 through an outlet of the ammonia pyrolysis heater 9, and denitration treatment is carried out on the flue gas.
An ammonia buffer tank 11 is further provided between the gasification tank 6 and the ammonia cracking tank 7, and the ammonia buffer tank 11 is used for storing the gasified ammonia gas, so that stable supply of the ammonia gas to the ammonia cracking tank 7 is ensured. The inside or the outside of ammonia buffer tank 11 is equipped with ammonia pre-heater 12, and ammonia pre-heater 12 is the ammonia and the heat pipe of enclosing on ammonia buffer tank 11 outer wall, and calcination heat exchanger 13 is also connected to ammonia pre-heater 12, utilizes ammonia pre-heater 12 to preheat the ammonia, promotes ammonia cracker quick schizolysis ammonia, ensures the steady supply of hydrogen.
The hydrogen, the nitrogen and part of the uncleaved ammonia gas enter the burner for combustion, and the nitrogen and the oxygen are combined to form nitrogen oxides in a certain temperature range, but the temperature of the position where the nitrogen enters the decomposing furnace 1 and the rotary kiln 2 is outside the temperature range, so that the nitrogen oxides are not formed. The ammonia gas has the functions of removing nitrogen oxides and inhibiting the generation of nitrogen oxides, so that the nitrogen oxides generated by calcining the decomposing furnace 1 and the rotary kiln 2 can be reduced, the content of NOx in the flue gas after doping combustion is continuously reduced to 45mg/m through detection, and the NOx is reduced by 25% compared with the NOx before doping hydrogen, thereby meeting the requirement of ultra-low emission. The technical result can be applied to a thermoelectric unit of a coal-fired thermal power plant, a coal-fired heating boiler, an industrial kiln adopting natural gas and a metal smelting furnace in the metallurgical industry besides being applied to a cement production line.
In other embodiments, the ammonia cracking heater 9 may also be directly connected to the flue gas outlet of the decomposing furnace 1, a part of flue gas directly enters the ammonia cracking heater 9 to heat and crack ammonia gas, and another part of flue gas enters the raw material preheater 3 to heat and preheat raw materials.
The working process of the utility model is as follows:
raw meal firstly passes through a raw meal preheater 3, high-temperature flue gas generated by a decomposing furnace 1 is preheated and then enters the decomposing furnace 1 for calcination, the raw meal calcined by the decomposing furnace 1 enters a rotary kiln 2 for calcination to form clinker, after the calcining heat exchangers 13 on the outer walls of the decomposing furnace 1 and the rotary kiln 2 absorb heat, the calcining heat exchangers 13 are heated and gasified, water vapor enters a liquid ammonia heater 8 to heat liquid ammonia in a gasification tank 6 for gasification, gasified ammonia enters an ammonia buffer tank 11 through a pipeline with a one-way valve, ammonia in the ammonia buffer tank 11 enters an ammonia pyrolysis tank 7 through a pipeline with a one-way valve, flue gas exhausted from the decomposing furnace 1 firstly passes through the raw meal preheater 3, flue gas after the raw meal is preheated enters a flue gas header 4, part of flue gas in the flue gas header 4 enters an ammonia pyrolysis heater 9 for heating ammonia in the ammonia pyrolysis tank 7 for pyrolysis to form hydrogen and nitrogen, the hydrogen and the nitrogen and part of the ammonia which are not cracked enter a combustor for combustion, the flue gas header 4 is connected with an outlet of the ammonia pyrolysis heater 9 for flue gas denitration treatment device 10 for denitration treatment.
Industrial production devices or production lines such as kilns, boilers, thermoelectric units, metal smelting furnaces and the like which take coal or natural gas as main fuel, such as cement kilns and decomposing furnaces, coal-fired boilers, coal-fired power generation units, secondary aluminum smelting furnaces and the like, can adopt the technology of replacing coal by using the ammonia to supply hydrogen. Under the background of double carbon, hydrogen energy is the first clean energy in the energy industry at present, but suffers from a plurality of adverse factors such as low hydrogen energy density, high storage and transportation cost, high risk and the like, and the search for a hydrogen storage medium which is free of carbon, easy to store and transport and high in use safety performance is an important task for ensuring the sustainable development of the hydrogen energy industry. Liquid ammonia is a chemical substance which contains no carbon, has high energy density, low maturation cost of storage and transportation technology and small use danger. Although liquid ammonia has many advantages compared with liquid hydrogen, the ignition temperature of ammonia gas is up to more than 650 ℃ and combustion is unstable, and the liquid ammonia is a technical bottleneck for industrial production as new energy. The utility model provides a technology for stable combustion of hydrogen supplied by ammonia pyrolysis, which is easy to control the working temperature required by cement industry at 900-1700 ℃ by adjusting the hydrogen-ammonia ratio, and can be used for adding hydrogen-ammonia fuel by only upgrading and refitting the existing production line with low intensity.
The benefit of the whole ammonia pyrolysis hydrogen supply coal reduction and carbon reduction technology is calculated by taking a decomposing furnace as an example, the single pyrolysis power of the decomposing furnace 1 is 150MW (combined with power generation), and if ammonia hydrogen supply is adopted to replace 20% of coal, the coal reduction is about 3.8 ten thousand tons (standard coal) per single year, and the emission of the corresponding carbon dioxide is about 15 ten thousand tons. According to the calculation of the recent carbon trade price of 60 yuan/ton, the cost of 900 ten thousand yuan coal fuel can be counteracted, the coal and carbon reduction can be greatly reduced in a cement plant, the carbon trade income can be obtained, the low-carbon green development of the cement industry can be effectively driven, the development of upstream and downstream related industries can be promoted by radiation, the income of related enterprises and staff can be increased, and the local economic development and the social stability can be strongly promoted.
The above description is only of the preferred embodiments of the present utility model and is not intended to limit the utility model in any way, and any person skilled in the art may make modifications or alterations to the equivalent embodiments using the technical disclosure described above. However, any simple modification, equivalent variation and variation of the above embodiments according to the technical substance of the present utility model still fall within the protection scope of the technical solution of the present utility model.
Claims (10)
1. An apparatus for replacing coal with ammonia and hydrogen in a cement clinker production line is characterized in that: the device comprises a cement clinker production line, a liquid ammonia storage tank (5), a liquid ammonia gasification device and an ammonia cracking device, wherein the liquid ammonia storage tank (5) is connected with a liquid ammonia gasification mechanism, the liquid ammonia gasification mechanism is connected with the ammonia cracking device, and the ammonia cracking device is connected to a combustor in the cement clinker production line through a hydrogen supply pipeline (14).
2. The apparatus for replacing coal with ammonia in hydrogen in a cement clinker production line according to claim 1, wherein: the combustor comprises a decomposing furnace hydrogen combustor (102) and a rotary kiln hydrogen combustor (202), wherein the decomposing furnace hydrogen combustor (102) is arranged on a decomposing furnace (1) of a cement clinker production line, and the rotary kiln hydrogen combustor (202) is arranged on a rotary kiln (2) of the cement clinker production line.
3. The apparatus for replacing coal with ammonia hydrogen in a cement clinker production line according to claim 2, wherein: a plurality of decomposing furnace hydrogen burners (102) are arranged in both the horizontal direction and the vertical direction of the decomposing furnace (1).
4. The apparatus for replacing coal with ammonia hydrogen in a cement clinker production line according to claim 2, wherein: a plurality of rotary kiln hydrogen burners (202) are axially arranged on the rotary kiln (2).
5. The apparatus for replacing coal with ammonia in hydrogen in a cement clinker production line according to claim 1, wherein: the liquid ammonia gasification device comprises a gasification tank (6) and a liquid ammonia heater (8), wherein a calcination heat exchanger (13) is arranged on the outer wall of a decomposing furnace (1) and/or a rotary kiln (2) of the cement clinker production line, and the calcination heat exchanger (13) is connected with the liquid ammonia heater (8) through a heat exchange pipeline.
6. The apparatus for replacing coal with ammonia hydrogen in a cement clinker production line according to claim 5, wherein: an ammonia buffer tank (11) is also arranged between the liquid ammonia gasification device and the ammonia cracking device.
7. The apparatus for replacing coal with ammonia hydrogen in a cement clinker production line according to claim 6, wherein: an ammonia preheater (12) is arranged on the inner side or the outer side of the ammonia buffer tank (11), and the ammonia preheater (12) is connected with a calcination heat exchanger (13).
8. An apparatus for replacing coal with ammonia hydrogen in a cement clinker production line according to claim 1 or 6, characterized in that: the ammonia pyrolysis device comprises an ammonia pyrolysis tank (7) and an ammonia pyrolysis heater (9), wherein the ammonia pyrolysis heater (9) is arranged on the inner side or the outer side of the ammonia pyrolysis tank (7), and the ammonia pyrolysis heater (9) is communicated with a flue gas outlet of a decomposing furnace (1) of the cement clinker production line.
9. The apparatus for replacing coal with ammonia hydrogen in a cement clinker production line according to claim 8, wherein: the flue gas outlet of the decomposing furnace (1) is connected with a plurality of raw material preheaters (3), the heat exchange flue gas outlet of the raw material preheaters (3) is connected with a flue gas collecting pipe (4), and the inlet of the ammonia pyrolysis heater (9) is connected with the flue gas collecting pipe (4).
10. The apparatus for replacing coal with ammonia hydrogen in a cement clinker production line according to claim 9, wherein: the flue gas collecting pipe (4) is connected with the flue gas denitration treatment device (10) through an outlet of the ammonia pyrolysis heater (9).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN119436093A (en) * | 2024-12-23 | 2025-02-14 | 合肥综合性国家科学中心能源研究院(安徽省能源实验室) | A thermal power deep peak regulation system and method based on ammonia cracking hydrogen production coupled with deep utilization of waste heat |
| BE1032762B1 (en) * | 2024-07-10 | 2026-02-09 | thyssenkrupp Polysius GmbH | Process for the thermal treatment of a mineral material in the cement, lime, residue and/or basic materials industry; ammonia as the main fuel |
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2023
- 2023-02-20 CN CN202320248380.5U patent/CN219156784U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE1032762B1 (en) * | 2024-07-10 | 2026-02-09 | thyssenkrupp Polysius GmbH | Process for the thermal treatment of a mineral material in the cement, lime, residue and/or basic materials industry; ammonia as the main fuel |
| CN119436093A (en) * | 2024-12-23 | 2025-02-14 | 合肥综合性国家科学中心能源研究院(安徽省能源实验室) | A thermal power deep peak regulation system and method based on ammonia cracking hydrogen production coupled with deep utilization of waste heat |
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