Clinker production system and method for full-oxygen combustion coupling carbon capture and waste heat power generation

Abstract

The invention discloses a clinker production system and method for full-oxygen combustion coupling carbon capture and waste heat power generation, and relates to the field of carbon reduction extension processes in the cement generation process, the clinker production system comprises a cement clinker firing system and a raw material grinding system, and further comprises a cryogenic carbon capture subsystem, a full-oxygen combustion subsystem and a waste heat power generation subsystem; the cryogenic carbon capture subsystem comprises a condensing tower, a gaseous carbon dioxide storage device and a liquid sulfur dioxide storage tank. By constructing an independent oxygen-fuel combustion subsystem, mutual coupling of oxygen-fuel combustion and alternative fuel and optimization of the proportion of oxygen and the alternative fuel, accurate control over the combustion temperature (for example, the temperature of an outlet in the top of a decomposing furnace is controlled to be 880-890 DEG C) is achieved, the fuel utilization rate is increased, generation of nitrogen oxide is reduced, nitrogen dilution is reduced through oxygen-fuel combustion, and the combustion efficiency is improved. The flame temperature and the heat efficiency are improved, and the alternative fuel utilization rate reaches 100%.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of carbon reduction in cement production process, in particular to a clinker production system and method of full-oxygen combustion coupled with carbon capture and waste heat power generation. BACKGROUND

[0002] As an important basic raw material industry in the world, the clinker production process of cement industry is accompanied by a large amount of energy consumption and pollutant emission. Data shows that the global cement industry carbon dioxide emissions account for about 8% of the total industrial emissions. At the same time, the pollutants such as sulfur dioxide and nitrogen oxides emitted in the traditional cement production process also have a significant impact on the atmospheric environment. With the increasingly stringent environmental protection standards, it is an urgent need for the industry to develop efficient and low-emission clinker production technology.

[0003] However, the existing equipment has the following problems: problem 1 combustion system energy efficiency and emission problem; the carbon dioxide concentration in the traditional cement clinker sintering system kiln tail gas is low (usually less than 20%), which increases the difficulty of subsequent carbon capture, and the high-temperature combustion process is easy to generate nitrogen oxides, which needs additional denitration treatment, increasing the cost. Although some enterprises try to introduce pure oxygen combustion technology to improve the carbon dioxide concentration, the existing full-oxygen combustion system has problems such as poor fuel adaptability and insufficient combustion temperature control precision, especially when using alternative fuels (such as biomass waste fuel and hazardous waste derived fuel), which is easy to cause combustion efficiency fluctuation, problem 2 carbon capture technology bottleneck and defects; the current industrial carbon capture mainly includes chemical absorption method, physical adsorption method and deep cooling separation method. The chemical absorption method has problems such as high energy consumption of absorbent regeneration and serious equipment corrosion; the physical adsorption method is limited by the adsorbent capacity and is difficult to adapt to the complex composition of cement kiln flue gas (containing sulfur dioxide, dust and other impurities); although the deep cooling separation method is suitable for high-concentration carbon dioxide gas treatment, the separation efficiency of sulfur dioxide and carbon dioxide is low when the traditional deep cooling device handles sulfur-containing flue gas, which is easy to cause equipment blockage or refrigerant pollution, and the energy consumption is high, problem 3; the waste heat is not fully utilized; in the cement production process, the kiln tail gas temperature is usually 250-350℃, the existing waste heat power generation system mostly uses steam cycle, which can only recover part of the sensible heat, and the low-temperature waste heat (such as the cold energy released in the deep cooling carbon capture process) is not fully utilized. At the same time, although the closed cycle power generation technology using carbon dioxide as the working medium has been studied, the integration degree with the cement production system is low, and the efficient energy coupling has not been formed, problem 4: the system lacks coordination; in the traditional clinker production system, the raw material grinding, sintering, environmental protection treatment and waste heat utilization links are relatively independent, and lack of systematic optimization. For example, the desulfurization and denitration process and the material mixing efficiency of raw material grinding are low, resulting in large consumption of desulfurizing agent; the oxygen supply of the carbon capture system and the combustion system does not form a closed loop, increasing the energy consumption of air oxygen production. Therefore, we developed a clinker production system and method of full-oxygen combustion coupled with carbon capture and waste heat power generation. SUMMARY

[0004] In view of the deficiencies of the existing clinker production system and method of waste heat power generation, the present application provides a clinker production system and method of waste heat power generation coupled with full-oxygen combustion and carbon capture, which has the advantages of independent full-oxygen combustion subsystem, mutual coupling of full-oxygen combustion and alternative fuel, optimization of oxygen and alternative fuel ratio, precise control of combustion temperature (such as controlling the outlet temperature of the top of the decomposition furnace at 880-890 DEG C), improved fuel utilization rate and reduced generation of nitrogen oxides, thereby solving the problems in the above background art.

[0005] The present application provides the following technical scheme: a clinker production system of waste heat power generation coupled with full-oxygen combustion and deep cold carbon capture, comprising a cement clinker firing system, a raw material grinding system, a deep cold carbon capture subsystem, a full-oxygen combustion subsystem, and a waste heat power generation subsystem.

[0006] The deep cold carbon capture subsystem comprises a condensation tower, a gaseous carbon dioxide storage device, a liquid sulfur dioxide storage tank, a sulfur dioxide liquefaction device, a gas compressor station, a carbon dioxide liquefaction device, a liquid carbon dioxide storage tank, and an air-to-liquid oxygen system; the outlet of the gaseous carbon dioxide storage device is connected to the first gas inlet of the sulfur dioxide liquefaction device through a pipeline, the inlet of the gaseous carbon dioxide storage device is connected to the outlet of the condensation tower through a pipeline, and the inlet of the gaseous carbon dioxide storage device is connected to the second steam turbine through a pipeline; the inlet of the condensation tower is connected to the outlet of the kiln tail exhaust fan through a pipeline; the outlet of the gas compressor station is connected to the second gas inlet of the carbon dioxide liquefaction device through a pipeline;

[0007] The full-oxygen combustion subsystem comprises an oxygen storage device, a first combustor, a second alternative fuel bin, and a sixth control valve, which are connected in sequence through pipelines; the first combustor is connected to the kiln head cover; the second alternative fuel bin is connected to the decomposition furnace, and the oxygen storage device is connected to the decomposition furnace through a pipeline;

[0008] The waste heat power generation subsystem comprises a waste heat power generation boiler, a condenser, a first steam turbine, an energy release heat exchanger, and a second steam turbine.

[0009] Preferably, the sulfur dioxide liquefaction device is composed of a first inner cavity and a first outer cavity, a first gas inlet is arranged at the top of the sulfur dioxide liquefaction device, the first gas inlet communicates with the first inner cavity through the first outer cavity, a first liquid oxygen inlet is arranged at the middle of the first outer cavity, a first oxygen outlet is arranged at the upper part of the first outer cavity, a liquid sulfur dioxide outlet is arranged at the bottom of the sulfur dioxide liquefaction device, an oxidized carbon outlet is arranged at the lower side of the first inner cavity, the first liquid oxygen inlet of the sulfur dioxide liquefaction device is connected with an air-made liquid oxygen system through a pipeline, the first oxygen outlet is connected with an oxygen storage device through a pipeline, the first gas inlet is connected with a gaseous carbon dioxide storage device through a pipeline, the liquid sulfur dioxide outlet is connected with a liquid sulfur dioxide storage tank through a pipeline, and the oxidized carbon outlet is connected with a gas compressor station inlet through a pipeline.

[0010] Preferably, the carbon dioxide liquefaction device is composed of a second inner cavity and a second outer cavity, a second gas inlet is arranged at the top and communicates with the second inner cavity through the second outer cavity, a second liquid oxygen inlet is arranged at the middle of the second outer cavity, a second oxygen outlet is arranged at the upper part of the second outer cavity, a liquid carbon dioxide outlet is arranged at the lower side of the second inner cavity, the second liquid oxygen inlet of the carbon dioxide liquefaction device is connected with an air-made liquid oxygen system through a pipeline, the second oxygen outlet is connected with an oxygen storage device through a pipeline, and the liquid carbon dioxide outlet is connected with a liquid carbon dioxide storage tank through a pipeline.

[0011] Preferably, the waste heat power generation boiler is sequentially provided with a carbon dioxide working medium evaporator, an economizer, an evaporator, a steam drum and a superheater from bottom to top; the economizer, the evaporator and the superheater are respectively connected with the steam drum through pipelines, the superheater is connected with a first steam turbine through a pipeline, the first steam turbine is connected with a condenser through a pipeline, the condenser is connected with the economizer through a pipeline, the carbon dioxide working medium evaporator is sequentially connected with an energy-releasing heat exchanger and a second steam turbine through pipelines, and the waste heat power generation boiler is connected with a liquid carbon dioxide storage tank through a pipeline.

[0012] Preferably, the cement kiln system comprises a preheater, a decomposing furnace, a flue, a rotary kiln, a kiln head cover, a grate cooler, a first alternative fuel bin, a second burner, a tertiary air pipe, a first cooling device, a second cooling device, a first dust collector, a first fan, a desulfurization device, a denitration device, a kiln inlet elevator, a humidification tower, a first control valve, a second control valve, a third control valve, a fourth control valve, a fifth control valve and a high-temperature fan; the denitration device is connected to the upper part of the decomposing furnace; the discharge outlet of the desulfurization device is divided into two paths, one of which is connected to the pipeline between the first cooling device and the second cooling device, and the powdered desulfurization material enters the first dust collector through the pipeline, and the other is connected to the kiln inlet elevator, and the powdered desulfurization material enters the preheater through the kiln inlet elevator; the flue gas outlet pipeline at the top of the preheater is divided into two paths and connected to the humidification tower and the waste heat power generation boiler respectively, and the first control valve and the second control valve are arranged on the pipeline respectively.

[0013] Preferably, the raw material grinding system comprises a raw material mill, a cyclone dust collector, a second dust collector, a zipper machine and a kiln tail fan; the zipper machine is provided with two inlets connected to the outlets of the cyclone dust collector and the second dust collector respectively, and the outlet of the zipper machine is connected to the kiln inlet elevator.

[0014] Preferably, the sulfur dioxide liquefaction device and the carbon dioxide liquefaction device are a single device or a matrix composed of several devices; the sulfur dioxide liquefaction device further comprises a first internal cavity temperature and pressure sensor and a first external cavity temperature and pressure sensor; the carbon dioxide liquefaction device further comprises a second internal cavity temperature and pressure sensor and a second external cavity temperature and pressure sensor.

[0015] The clinker production method of full-oxygen combustion coupled with deep cooling carbon capture and waste heat power generation comprises the following operation steps:

[0016] S1: clinker production process, raw material grinding system grinds raw materials and transports them to the kiln inlet elevator through the zipper machine, enters the cement kiln system to calcine to produce cement clinker, the energy required for calcination is provided by oxygen and alternative fuel, the oxygen is prepared by the air liquid oxygen system, and the liquid oxygen is exchanged with the cryogenic carbon capture subsystem to generate oxygen, the oxygen enters the oxygen storage device through the pipeline, and then enters the cement clinker firing system in two ways, the first way of oxygen enters the first burner to provide 5%-10% of the energy for calcination of cement clinker, the second way of oxygen provides 0%-5% of the energy for calcination of cement clinker by adjusting the opening of the sixth control valve to provide oxygen combustion in the decomposing furnace, the alternative fuel in the first alternative fuel bin is transported to the second burner, and the second burner burns the alternative fuel to provide 55%-60% of the energy for calcination of cement clinker; the second alternative fuel bin directly feeds the alternative fuel into the decomposing furnace, providing 40%-45% of the energy for the cement clinker firing system; the alternative fuel is a mixture of biomass waste fuel, hazardous waste derived fuel, and hazardous solid waste fuel, with a calorific value of 20GJ / T-25GJ / T; during operation, the operating temperature at the position where the decomposing furnace bottom is connected with the flue is controlled between 1000°C-1100°C, and the outlet temperature at the top of the decomposing furnace is controlled between 880°C-890°C; the temperature distribution in the rotary kiln is as follows: the temperature at the connection between the kiln head cover and the rotary kiln is controlled between 1600°C-1700°C, the temperature in the middle of the rotary kiln is controlled between 1200°C-1300°C, and the operating temperature at the position where the rotary kiln is connected with the flue is controlled between 1100°C-1200°C; during operation, the high-temperature flue gas temperature at the top of the preheater outlet pipe is controlled between 250°C-350°C, and the high-temperature flue gas enters the waste heat power generation boiler under the negative pressure provided by the high-temperature fan to provide heat energy for power generation.

[0017] S2: desulfurization and denitrification process, in the S1 clinker production process, the denitrification solution is pumped into the decomposing furnace through the denitrification device and pipeline, and reacts with the material at high temperature in the decomposing furnace to remove nitrogen oxides, i.e. the denitrification process; the desulfurization powder in the desulfurization device enters the kiln inlet elevator through the pipeline and mixes with the ground raw materials, and then enters the preheater, and reacts with the material at high temperature in the preheater to remove sulfides, and the other way of desulfurization powder enters the first dust collector, and mixes with the material in the first dust collector; the high-temperature flue gas after desulfurization and denitrification still contains a small amount of sulfur dioxide, water vapor and dust containing carbon dioxide.

[0018] S3: Cryogenic carbon capture process, after the desulfurization and denitrification of the high-temperature flue gas in the S2 step, the high-temperature flue gas is cooled by the water spray in the humidification tower under the negative pressure provided by the high-temperature fan, and then enters the raw material grinding system. The high-temperature flue gas after removing dust in the second dust collector only contains a small amount of sulfur dioxide, water vapor and carbon dioxide. The high-temperature flue gas after removing dust enters the cryogenic carbon capture subsystem under the negative pressure provided by the kiln tail exhaust fan. In the cryogenic carbon capture subsystem, the water vapor is first removed by the condensation tower, and then enters the gaseous carbon dioxide storage device for storage. After reaching the specified pressure, it enters the sulfur dioxide liquefaction device, where the sulfur dioxide is liquefied to form sulfuric acid. The sulfuric acid enters the liquid sulfur dioxide storage tank. At this time, the high-temperature flue gas from the kiln tail preheater only contains normal pressure carbon dioxide gas. The normal pressure carbon dioxide gas enters the gas compressor station and is compressed into high pressure carbon dioxide gas, which is then liquefied into liquid carbon dioxide in the carbon dioxide liquefaction device and stored in the liquid carbon dioxide storage tank, completing the carbon dioxide capture.

[0019] S4: Waste heat power generation process of liquid carbon dioxide, the liquid carbon dioxide generated after the low-temperature carbon capture process in step S3 enters the waste heat power generation subsystem and is gasified into high-pressure gaseous carbon dioxide in the carbon dioxide working medium evaporator in the waste heat power generation boiler. The high-pressure gaseous carbon dioxide enters the energy-releasing heat exchanger, where it is heated and forms high-temperature and high-pressure gaseous carbon dioxide. The high-temperature and high-pressure gaseous carbon dioxide enters the second steam turbine to release energy and drive the steam turbine to rotate, which in turn drives the electric motor to generate electricity. The gaseous carbon dioxide after releasing energy becomes normal temperature and pressure carbon dioxide gas, which is returned to the gaseous carbon dioxide storage device for storage, thereby forming a carbon dioxide power generation cycle system.

[0020] S5: Waste heat power generation process of kiln tail high-temperature flue gas, in the S1 clinker production process, when the second control valve, the fourth control valve and the fifth control valve are opened at the same time, the kiln tail high-temperature flue gas from the top outlet of the preheater enters the waste heat power generation boiler. Water enters the waste heat power generation boiler through the economizer and is heated by the high-temperature flue gas to form superheated steam. The superheated steam enters the first steam turbine to drive the turbine to rotate and generate electricity. At the same time, the superheated steam releases energy and cools down, and then enters the condenser through the first steam turbine. The superheated steam is condensed into water in the condenser, and then returns to the waste heat power generation boiler through the pipeline, forming a waste heat power generation cycle system using the kiln tail high-temperature flue gas.

[0021] Preferably, in the S3 deep cold carbon capture process, by controlling the amount of liquid oxygen supply and real-time monitoring of the temperature and pressure of the first internal cavity temperature and pressure sensor of the sulfur dioxide liquefaction device, the temperature inside the first internal cavity is controlled at-10℃ and the pressure is controlled at normal pressure, in this state, the sulfur dioxide is liquefied and enters the liquid sulfur dioxide storage tank, while the carbon dioxide continues to remain in a gaseous state and continues to enter the gas compressor station, through this process, a small amount of residual sulfur dioxide in the high-temperature flue gas at the kiln tail is separated and removed.

[0022] Preferably, in the S3 deep cold carbon capture process, by controlling the amount of liquid oxygen supply and real-time monitoring of the temperature and pressure of the first internal cavity temperature and pressure sensor of the sulfur dioxide liquefaction device, the temperature inside the first internal cavity is controlled at-10℃ and the pressure is controlled at normal pressure, in this state, the sulfur dioxide is liquefied and enters the liquid sulfur dioxide storage tank, while the carbon dioxide continues to remain in a gaseous state and continues to enter the gas compressor station, through this process, a small amount of residual sulfur dioxide in the high-temperature flue gas at the kiln tail is separated and removed.

[0023] Compared with the prior art, the present application has the following beneficial effects:

[0024] 1. By constructing an independent full-oxygen combustion subsystem, the full-oxygen combustion and the alternative fuel are coupled with each other, the ratio of oxygen and alternative fuel is optimized, the combustion temperature is accurately controlled (such as the outlet temperature at the top of the decomposition furnace is controlled at 880-890℃), the fuel utilization rate is improved and the generation of nitrogen oxides is reduced, the full-oxygen combustion reduces the dilution of nitrogen, improves the flame temperature and thermal efficiency, and the utilization rate of alternative fuel reaches 100%.

[0025] 2. By designing a double-cavity structure for step-by-step liquefaction of sulfur dioxide and carbon dioxide (such as sulfur dioxide liquefaction device and carbon dioxide liquefaction device), and by coupling the deep cold carbon capture system with the full-oxygen combustion system to realize the step-by-step utilization of liquid oxygen cold energy, the sulfur dioxide is separated at normal pressure-10℃ and the carbon dioxide is liquefied at 0.6MPa-50℃, solving the problem of impurity interference in traditional deep cold devices and improving the carbon capture efficiency to more than 90%.

[0026] 3. By establishing a dual-power generation system of carbon dioxide working medium closed cycle and steam cycle, not only the high-temperature waste heat of the kiln tail flue gas is recovered, but also the liquid carbon dioxide gasification process is used to drive the steam turbine to generate electricity, forming a high-efficiency conversion of "thermal energy-mechanical energy-electric energy", and the power generation efficiency is expected to be improved by 15% to 20% compared with the traditional system.

[0027] 4. By integrating the raw material grinding, sintering, environmental protection treatment and energy recovery links, and by real-time regulation and control through temperature and pressure sensors (such as internal temperature and pressure control of the sulfur dioxide liquefaction device), the deep coupling of material flow, energy flow and information flow is realized, and the system energy consumption and pollutant emissions are reduced.

[0028] 5、By the transformation of the existing cement production line, only need to make small-scale transformation to the decomposing furnace, alternative fuel burner and so on, full-oxygen combustion can be realized, the deep cooling carbon capture system and the waste heat power generation system can be directly modularized into the existing cement production line, the system modification workload is small, the transformation cost is low, the economy is good, and the adaptability is strong. BRIEF DESCRIPTION OF DRAWINGS

[0029] Figure 1 The production process chart of the present application is provided;

[0030] Figure 2 The deep cooling carbon capture subsystem flow chart of the present application is provided;

[0031] Figure 3 The full-oxygen combustion subsystem flow chart of the present application is provided;

[0032] Figure 4 The waste heat power generation subsystem flow chart of the present application is provided;

[0033] Figure 5 The sulfur dioxide liquefaction device chart of the present application is provided;

[0034] Figure 6 The carbon dioxide liquefaction device chart of the present application is provided;

[0035] Figure 7 The waste heat power generation boiler device chart of the present application is provided.

[0036] In the figure: 1, preheater; 2, decomposition furnace; 3, flue chamber; 4, rotary kiln; 5, kiln head cover; 6, grate cooler; 7, first alternative fuel bin; 8, first burner; 9, second burner; 10, tertiary air pipe; 11, second alternative fuel bin; 12, first cooling device; 13, second cooling device; 14, first dust collector; 15, first fan; 16, desulfurization device; 17, denitration device; 18, kiln inlet elevator; 19, humidification tower; 20, first control valve; 21, second control valve; 22, third control valve; 23, fourth control valve; 24, fifth control valve; 25, waste heat power generation boiler; 251, carbon dioxide working medium evaporator; 252, coal economizer; 253, evaporator; 254, steam drum; 255, superheater; 26, condenser; 27, first steam turbine; 28, energy release heat exchanger; 29, second steam turbine; 30, high-temperature fan; 31, raw material mill; 32, cyclone dust collector; 33, second dust collector; 34, zipper machine; 35, kiln tail exhaust fan; 36, condensing tower; 37, gaseous carbon dioxide storage device; 38, liquid sulfur dioxide storage tank; 39, sulfur dioxide liquefaction device; 391, first gas inlet; 392, first oxygen outlet; 393, first liquid oxygen inlet; 394, oxidized carbon outlet; 395, liquid sulfur dioxide outlet; 396, first internal cavity; 397, first external cavity; 398, first internal cavity temperature and pressure measuring sensor; 399, first external cavity temperature and pressure measuring sensor; 40, gas compressor station; 41, carbon dioxide liquefaction device; 411, second gas inlet; 412, second oxygen outlet; 413, second liquid oxygen inlet; 414, liquid carbon dioxide outlet; 415, second internal cavity; 416, second external cavity; 417, second internal cavity temperature and pressure measuring sensor; 418, second external cavity temperature and pressure measuring sensor; 42, liquid carbon dioxide storage tank; 43, air-to-liquid oxygen system; 44, oxygen storage device; 45, sixth control valve. DETAILED DESCRIPTION

[0037] Example 1

[0038] Taking a 5000 tons of clinker production line as an example, the clinker production system coupled with full-oxygen combustion and deep cold carbon capture and waste heat power generation includes a cement clinker firing system and a raw material grinding system, and further includes a deep cold carbon capture subsystem, a full-oxygen combustion subsystem, and a waste heat power generation subsystem.

[0039] The deep cold carbon capture subsystem includes a condensing tower 36, a gaseous carbon dioxide storage device 37, a liquid sulfur dioxide storage tank 38, a sulfur dioxide liquefaction device 39, a gas compressor station 40, a carbon dioxide liquefaction device 41, a liquid carbon dioxide storage tank 42, and an air-to-liquid oxygen system 43.

[0040] Specifically, the sulfur dioxide liquefaction device 39 is composed of a first inner cavity 396 and a first outer cavity 397, a first gas inlet 391 is arranged at the top and communicates with the first inner cavity 396 through the first outer cavity 397, a first liquid oxygen inlet 393 is arranged at the middle position of the first outer cavity 397, a first oxygen outlet 392 is arranged at the upper part of the first outer cavity 397, a liquid sulfur dioxide outlet 395 is arranged at the bottom, an oxidized carbon outlet 394 is arranged at the lower side of the first inner cavity 396, the first liquid oxygen inlet 393 of the sulfur dioxide liquefaction device 39 is connected with the air-made liquid oxygen system 43 through a pipeline, the first oxygen outlet 392 is connected with the oxygen storage device 44 through a pipeline, the first gas inlet 391 is connected with the gaseous carbon dioxide storage device 37 through a pipeline, the liquid sulfur dioxide outlet 395 is connected with the liquid sulfur dioxide storage tank 38 through a pipeline, and the oxidized carbon outlet 394 is connected with the inlet of the gas compressor station 40 through a pipeline;

[0041] Exemplarily, the sulfur dioxide liquefaction device 39 adopts three parallel matrix devices, the size of a single first inner cavity is φ2.5m*10m, a first inner cavity temperature and pressure measuring sensor 398 with an accuracy of ±0.5℃ and ±0.01MPa is arranged, the first outer cavity 397 is connected with the air-made liquid oxygen system 43 through a DN200 pipeline, the liquid oxygen flow is controlled at 20m 3 / h.

[0042] Specifically, the outlet of the gaseous carbon dioxide storage device 37 is connected with the first gas inlet 391 of the sulfur dioxide liquefaction device 39 through a pipeline, the inlet of the gaseous carbon dioxide storage device 37 is connected with the outlet of the condensing tower 36 through a pipeline, and the inlet of the gaseous carbon dioxide storage device 37 is connected with the second steam turbine 29 through a pipeline; the inlet of the condensing tower 36 is connected with the outlet of the kiln tail exhaust fan 35 through a pipeline; the carbon dioxide liquefaction device 41 is composed of a second inner cavity 415 and a second outer cavity 416, a second gas inlet 411 is arranged at the top and communicates with the second inner cavity 415 through the second outer cavity 416, a second liquid oxygen inlet 413 is arranged at the middle position of the second outer cavity 416, a second oxygen outlet 412 is arranged at the upper part of the second outer cavity 416, a liquid carbon dioxide outlet 414 is arranged at the lower side of the second inner cavity 415, the second liquid oxygen inlet 413 of the carbon dioxide liquefaction device 41 is connected with the air-made liquid oxygen system 43 through a pipeline, the second oxygen outlet 412 is connected with the oxygen storage device 44 through a pipeline, and the liquid carbon dioxide outlet 414 is connected with the liquid carbon dioxide storage tank 42 through a pipeline;

[0043] Exemplarily, the carbon dioxide liquefaction device 41: 2 sets of tandem devices are arranged, the second internal cavity size φ3m×15m, equipped with the second internal cavity temperature and pressure measuring sensor 417 with an accuracy of ±1℃, ±0.02MPa, the liquid oxygen inlet pipeline DN150, the liquid oxygen supply rate 15m 3 / h.

[0044] Specifically, the gas compressor station 40 outlet is connected with the second gas inlet 411 arranged in the carbon dioxide liquefaction device 41 and communicated through the pipeline;

[0045] Exemplarily, the gas compressor station 40: 3 centrifugal compressors are arranged, and a single unit has a rated processing capacity of 5000Nm 3 / h, the inlet pressure is normal pressure, and the outlet pressure is raised to 2.0MPa.

[0046] The oxy-combustion subsystem includes: an oxygen storage device 44, a first combustor 8, a second alternative fuel bin 11 and a sixth control valve 45 and is sequentially connected through the pipeline;

[0047] Specifically, the first combustor 8 is connected with the kiln head cover 5; the second alternative fuel bin 11 is connected with the decomposing furnace 2, and the oxygen storage device 44 is connected with the decomposing furnace 2 through the pipeline;

[0048] Exemplarily, the oxygen storage device 44: the volume is 2000m 3 , the storage pressure is 8MPa, the oxygen supply pipeline is divided into two ways: the first way DN100 pipeline to the first combustor 8, the flow rate is 500Nm 3 / h, and 8% of the calcination energy is provided; the second way DN80 pipeline to the decomposing furnace 2, the flow rate is adjusted to 200Nm 3 / h through the sixth control valve 45, and 3% of the energy is provided.

[0049] The waste heat power generation subsystem includes: a waste heat power generation boiler 25, a condenser 26, a first steam turbine 27, an energy release heat exchanger 28 and a second steam turbine 29.

[0050] Specifically, the waste heat power generation boiler 25 is sequentially provided with a carbon dioxide working medium evaporator 251, an economizer 252, an evaporator 253, a steam drum 254 and a superheater 255 from the lower part to the upper part.

[0051] Specifically, the economizer 252, the evaporator 253 and the superheater 255 are respectively connected with the steam drum 254 through the pipeline, the superheater 255 is connected with the first steam turbine 27 through the pipeline, the first steam turbine 27 is connected with the condenser 26 through the pipeline, the condenser 26 is connected with the economizer 252 through the pipeline, the carbon dioxide working medium evaporator 251 is connected with the energy release heat exchanger 28, and the second steam turbine 29 is sequentially connected through the pipeline, and the waste heat power generation boiler 25 is connected with the liquid carbon dioxide storage tank 42 through the pipeline.

[0052] Exemplarily, the waste heat power generation boiler 25: carbon dioxide working medium evaporator 251 heat exchange area 1500 square meters, coal economizer 252 / evaporator 253 / overheater 255 respectively with 80m 3 The steam drum 254 is connected, and the superheated steam parameters are: pressure 3.5 MPa, temperature 450℃, corresponding to the rated power of the first steam turbine 27 5MW.

[0053] Specifically, in the clinker production process, the raw material grinding system transports the ground raw material to the kiln inlet elevator 18 through the zipper machine 34, enters the cement kiln system for calcination to produce cement clinker, and the energy required in the calcination process is provided by oxygen and alternative fuel. Oxygen is generated by heat exchange between liquid oxygen prepared by an air-to-liquid oxygen system 43 and a cryogenic carbon capture subsystem, and the oxygen enters the oxygen storage device 44 through the pipeline, and then is divided into two paths to enter the cement clinker firing system. The first path of oxygen enters the first burner 8 to provide 5% to 10% of the energy for calcination of cement clinker, and the second path of oxygen provides oxygen combustion-supporting to the decomposing furnace 2 through the opening degree adjustment of the sixth control valve 45, and the second path of oxygen provides 0% to 5% of the energy for calcination of cement clinker. The alternative fuel in the first alternative fuel bin 7 is transported to the second burner 9, and the second burner 9 burns the alternative fuel to provide 55% to 60% of the energy for calcination of cement clinker; the second alternative fuel bin 11 directly feeds the alternative fuel into the decomposing furnace 2, which provides 40% to 45% of the energy for the cement clinker firing system; the alternative fuel is a mixture of biomass waste fuel, hazardous waste derived fuel, and hazardous solid waste fuel, and its calorific value is between 20GJ / T and 25GJ / T; during operation, the operating temperature at the position where the decomposing furnace 2 bottom is connected with the flue gas chamber 3 is controlled between 1000℃ and 1100℃, and the outlet temperature at the top of the decomposing furnace 2 is controlled between 880℃ and 890℃; the temperature distribution in the rotary kiln is as follows: the temperature at the position where the kiln head cover 5 is connected with the rotary kiln 4 is controlled between 1600℃ and 1700℃, the temperature in the middle of the rotary kiln 4 is controlled between 1200℃ and 1300℃, and the operating temperature at the position where the rotary kiln 4 is connected with the flue gas chamber 3 is controlled between 1100℃ and 1200℃; during operation, the high-temperature flue gas temperature at the top outlet of the preheater 1 is controlled between 250℃ and 350℃, and the high-temperature flue gas enters the waste heat power generation boiler 25 under the negative pressure provided by the high-temperature fan 30 to provide heat energy for power generation.

[0054] Specifically, the desulfurization and denitrification process, in the clinker production process, the denitrification solution is pumped into the decomposing furnace 2 through the denitrification device 17 and pipeline, and reacts with the material at high temperature in the decomposing furnace 2 to remove nitrogen oxides, that is, the denitrification process; the desulfurization powder in the desulfurization device 16 enters into the kiln elevator 18 through the pipeline and mixes with the ground raw materials, and then enters into the preheater 1, and reacts with the material at high temperature in the preheater 1 to remove sulfides; another way of desulfurization powder enters into the first dust collector 14 through the pipeline and mixes with the material in the first dust collector 14; the high-temperature flue gas after desulfurization and denitrification still contains a small amount of sulfur dioxide, water vapor and dust containing carbon dioxide.

[0055] Exemplarily, in the denitrification process, the denitrification device 17 sprays ammonia water with a concentration of 20%, the removal rate of NOx is 85%, and the outlet concentration is ≤10mg / Nm 3 .

[0056] Exemplarily, in the desulfurization process, 50% of the desulfurization powder CaO-based enters the preheater with the raw materials, and 50% enters the first dust collector, the removal rate of SO2 is 97%, and the outlet concentration is ≤10mg / Nm 3 .

[0057] Specifically, the deep cold carbon capture process, the high-temperature flue gas after desulfurization and denitrification is cooled by spraying water in the humidification tower 19 under the negative pressure provided by the high-temperature fan 30, and then enters the raw material grinding system, removes dust in the second dust collector 33, and the high-temperature flue gas after removing dust only contains a small amount of sulfur dioxide, water vapor and carbon dioxide, which enters the deep cold carbon capture subsystem under the negative pressure provided by the kiln tail exhaust fan 35, removes water vapor in the condensation tower 36, and then enters the gaseous carbon dioxide storage device 37 for storage, reaches the specified pressure, and then enters the sulfur dioxide liquefaction device 39, and the sulfur dioxide is liquefied into sulfuric acid in the sulfur dioxide liquefaction device 39, and the sulfuric acid enters the liquid sulfur dioxide storage tank 38, at this time, the high-temperature flue gas from the kiln tail preheater 1 only contains normal pressure carbon dioxide gas, which enters the gas compressor station 40 and is compressed into high-pressure carbon dioxide gas, and then enters the carbon dioxide liquefaction device 41 and is liquefied into liquid carbon dioxide, and then enters the liquid carbon dioxide storage tank 42 for storage, and the carbon dioxide capture is completed.

[0058] Specifically, in the process of cryogenic carbon capture, by controlling the amount of liquid oxygen supply and real-time monitoring of the temperature and pressure of the first internal cavity temperature and pressure sensor 398 of the sulfur dioxide liquefaction device 39, the temperature inside the first internal cavity 396 is controlled at-10℃ and the pressure is controlled at normal pressure, in this state, the sulfur dioxide is liquefied and enters the liquid sulfur dioxide storage tank 38, and the carbon dioxide continues to remain in the gaseous state and continues to enter the gas compressor station 40, through this process, a small amount of sulfur dioxide remaining in the kiln tail high-temperature flue gas is separated and removed.

[0059] Specifically, in the process of cryogenic carbon capture, by controlling the amount of liquid oxygen supply and real-time monitoring of the temperature and pressure of the first internal cavity temperature and pressure sensor 398 of the sulfur dioxide liquefaction device 39, the temperature inside the first internal cavity 396 is controlled at-10℃ and the pressure is controlled at normal pressure, in this state, the sulfur dioxide is liquefied and enters the liquid sulfur dioxide storage tank 38, and the carbon dioxide continues to remain in the gaseous state and continues to enter the gas compressor station 40, through this process, a small amount of sulfur dioxide remaining in the kiln tail high-temperature flue gas is separated and removed.

[0060] Specifically, in the process of cryogenic carbon capture, by controlling the amount of liquid oxygen supply and real-time monitoring of the temperature and pressure of the first internal cavity temperature and pressure sensor 398 of the sulfur dioxide liquefaction device 39, the temperature inside the first internal cavity 396 is controlled at-10℃ and the pressure is controlled at normal pressure, in this state, the sulfur dioxide is liquefied and enters the liquid sulfur dioxide storage tank 38, and the carbon dioxide continues to remain in the gaseous state and continues to enter the gas compressor station 40, through this process, a small amount of sulfur dioxide remaining in the kiln tail high-temperature flue gas is separated and removed.

[0061] Specifically, in the process of cryogenic carbon capture, the carbon dioxide capture rate is more than 95%.

[0062] Specific data are as follows:

[0063] The compressor outlet high-pressure CO2 2.0 MPa enters the liquefaction device, and the second internal cavity is controlled at-50℃ and 0.6 MPa;

[0064] The liquefaction efficiency is ≥95%;

[0065] The liquid CO2 storage rate is 20t / h.

[0066] Specifically, in the process of waste heat power generation of liquid carbon dioxide, the liquid carbon dioxide generated after the low-temperature carbon capture process enters the waste heat power generation system, and is gasified into high-pressure gaseous carbon dioxide in the carbon dioxide working medium evaporator 251 in the waste heat power generation boiler 25, and then enters the energy release heat exchanger 28, and after heating and warming up in the energy release heat exchanger 28, high-temperature and high-pressure gaseous carbon dioxide is formed, which enters the second steam turbine 29 to release energy and drive the steam turbine to rotate, and then drives the motor to generate electricity, and the gaseous carbon dioxide after releasing energy becomes normal-temperature and normal-pressure carbon dioxide gas, which returns to the gaseous carbon dioxide storage device 37 for storage, thereby forming a circulating system for carbon dioxide power generation.

[0067] Specifically, the kiln tail high-temperature flue gas waste heat power generation process, in the clinker production process, when the second control valve 21, the fourth control valve 23, the fifth control valve 24 are opened at the same time, the kiln tail high-temperature flue gas from the top outlet air pipe of the preheater 1 enters into the waste heat power generation boiler 25, the water enters into the waste heat power generation boiler 25 through the economizer 252, and forms superheated steam under the heating of the high-temperature flue gas, the superheated steam enters into the first steam turbine 27 through the pipeline to drive the steam turbine to rotate and generate electricity, at the same time, the superheated steam releases its own temperature after entering the condenser 26 through the first steam turbine 27, and becomes water inside the condenser 26, the water returns to the waste heat power generation boiler 25 through the pipeline, forming a waste heat power generation circulation system using the kiln tail high-temperature flue gas.

[0068] Exemplarily, the kiln tail flue gas waste heat power generation cycle efficiency is 32%, the carbon dioxide working medium cycle power generation efficiency is 18%, and the total power generation power is 7MW, which meets the 30% electricity demand of the production line.

[0069] Embodiment 2:

[0070] In the 8000 tons of clinker production line embodiment, the basic principles of the process system and the operation method in embodiment 1 are not changed.

[0071] System composition and equipment parameters are as follows:

[0072] Exemplarily, the deep cooling carbon capture subsystem, the sulfur dioxide liquefaction device 39: 5 parallel matrixes are adopted to cope with high-sulfur flue gas, the single first internal cavity is φ3m×12m, the pre-cooling section cooling medium-30℃ liquid nitrogen is additionally added, the liquid oxygen flow is increased to 35m 3 / h, the high-precision sensor temperature is ±0.3℃, and the pressure is ±0.005MPa

[0073] Exemplarily, the carbon dioxide liquefaction device 41: 4 series matrixes, the second internal cavity is φ4m×20m, the guide vane structure is optimized, the liquid oxygen supply rate is 25m 3 / h, and the outlet liquid CO2 purity is ≥99.9%.

[0074] The gaseous carbon dioxide storage device 37: the volume is 5000m 3 , the design pressure is 0.8MPa, and the inlet is connected with the condensing tower 36 and the second steam turbine 29 in double ways.

[0075] Exemplarily, the full-oxygen combustion subsystem, the oxygen storage device 44: the volume is 3500m 3 , the storage pressure is 10MPa, the first burner oxygen supply flow is 800Nm 3 / h, the energy proportion is 10%, the decomposition furnace oxygen supply flow is 300Nm 3 / h, and the energy proportion is 5%.

[0076] Exemplarily, the alternative fuel system: the first alternative fuel bin 7 mixes the hazardous solid waste fuel with a heat value of 25 GJ / T, accounting for 60%, and the biomass waste fuel accounting for 40%, and is burned at a rate of 18 t / h by the second burner, accounting for 55%; the second alternative fuel bin 11 feeds the hazardous waste-derived fuel with a heat value of 23 GJ / T at a rate of 15 t / h, accounting for 45%.

[0077] Exemplarily, the waste heat power generation system, the waste heat power generation boiler 25: the carbon dioxide working medium evaporator has a heat exchange area of 2500 m2, the superheater outlet steam parameter is 4.0 MPa, 500 DEG C, and the first steam turbine has a rated power of 8 MW; the energy release heat exchanger 28 adopts a plate structure, has a heat exchange efficiency of 92%, and the second steam turbine has a rated power of 3.5 MW.

[0078] Exemplarily, the raw material grinding system: the raw material mill 31 has a processing capacity of 200 t / h, the cyclone dust collector 32 has an efficiency of 98%, and the kiln tail exhaust fan 35 has a wind volume of 150000 Nm 3 / h.

[0079] Production method and process parameters:

[0080] Exemplarily, the clinker production process S1 temperature control: the bottom of the decomposing furnace is 1100 DEG C, and the top is 890 DEG C; the kiln head of the rotary kiln is 1700 DEG C, the middle part is 1300 DEG C, and the kiln tail is 1200 DEG C; the preheater outlet flue gas temperature is 350 DEG C, and the flue gas volume is 200000 Nm 3 / h.

[0081] Exemplarily, energy distribution: the total heat value of the alternative fuel accounts for 95%, and the oxygen combustion support provides 5% of the first burner + 0% of the decomposing furnace, the sixth control valve is fully closed, and the pure oxygen combustion mode is adapted.

[0082] Specifically, the cryogenic carbon capture process S3-S4

[0083] Exemplarily, sulfur dioxide separation: for high-sulfur flue gas with an initial SO2 concentration of 800 mg / Nm 3 , the first internal cavity of the liquefaction device is controlled at -12 DEG C and atmospheric pressure, the SO2 removal rate is 98%, and the liquid SO2 storage rate is 8 t / h.

[0084] Exemplarily, carbon dioxide liquefaction: the compressor outlet pressure is raised to 2.5 MPa, the second internal cavity of the liquefaction device is controlled at -55 DEG C and 0.7 MPa, the liquid CO2 storage rate is 35 t / h, and the large-scale capture demand of the CCUS project is met.

[0085] Exemplarily, waste heat power generation: the kiln tail flue gas power generation efficiency is 35%, the carbon dioxide working medium cycle efficiency is 20%, the total power generation power is 11.5 MW, and the self-power supply rate is 40%.

[0086] Exemplarily, desulfurization and denitrification process S2: denitrification process, SNCR+SCR combined process, NOx removal rate 95%, outlet concentration ≤30 mg / Nm 3 . Desulfurization process, 70% of desulfurization powder into preheater, 30% into dust collector, for high sulfur fuel sulfur content 3%, SO2 removal rate 92%, outlet concentration ≤20 mg / Nm 3 .

[0087] Exemplarily, special working condition control: when the raw material grinding system fails, switch 80% of the flue gas to the humidification tower 19 through the first control valve 20 to ensure the stability of the kiln system. The deep cooling system is provided with a redundant loop, and when a single liquefaction device fails, the remaining devices automatically increase the load to 120% to maintain the capture efficiency ≥90%.

[0088] Specifically, the deep cooling liquefaction is coupled with waste heat recovery

[0089] Exemplarily, -183 ℃ liquid oxygen is provided by the air-to-liquid oxygen system 43, and at the same time, the cold energy of the liquefaction process is recovered for CO2 working medium pre-cooling, and the cold energy recovery efficiency is improved by 40%.

Claims

1. A clinker production system coupled with oxy-fuel combustion, cryogenic carbon capture, and waste heat power generation, comprising a cement clinker calcination system and a raw material grinding system, characterized in that: It also includes a cryogenic carbon capture subsystem, an oxygen-fuel combustion subsystem, and a waste heat power generation system; The cryogenic carbon capture subsystem includes: a condenser tower (36), a gaseous carbon dioxide storage device (37), a liquid sulfur dioxide storage tank (38), a sulfur dioxide liquefaction device (39), a gas compressor station (40), a carbon dioxide liquefaction device (41), a liquid carbon dioxide storage tank (42), and an air-to-liquid oxygen system (43); the outlet of the gaseous carbon dioxide storage device (37) is connected to the first gas inlet (391) of the sulfur dioxide liquefaction device (39) through a pipeline, the inlet of the gaseous carbon dioxide storage device (37) is connected to the outlet of the condenser tower (36) through a pipeline, and the inlet of the gaseous carbon dioxide storage device (37) is connected to the second steam turbine (29) through a pipeline; the inlet of the condenser tower (36) is connected to the outlet of the kiln tail exhaust fan (35) through a pipeline; the outlet of the gas compressor station (40) is connected to the second gas inlet (411) of the carbon dioxide liquefaction device (41) through a pipeline; The all-oxygen combustion subsystem includes an oxygen storage device (44), a first burner (8), a second alternative fuel bin (11), and a sixth control valve (45), which are connected in sequence by pipes; the first burner (8) is connected to the kiln head hood (5); the second alternative fuel bin (11) is connected to the decomposition furnace (2); and the oxygen storage device (44) is connected to the decomposition furnace (2) by pipes. The waste heat power generation system includes: a waste heat power generation boiler (25), a condenser (26), a first steam turbine (27), an energy release heat exchanger (28), and a second steam turbine (29).

2. The clinker production system of all-oxygen combustion coupled with cryogenic carbon capture and waste heat power generation according to claim 1, characterized in that: The sulfur dioxide liquefaction device (39) consists of a first internal cavity (396) and a first external cavity (397). A first gas inlet (391) is provided at the top of the sulfur dioxide liquefaction device (39), which passes through the first external cavity (397) and communicates with the first internal cavity (396). A first liquid oxygen inlet (393) is provided in the middle of the first external cavity (397), and a first oxygen outlet (392) is provided at the upper part of the first external cavity (397). A liquid sulfur dioxide outlet (393) is provided at the bottom of the sulfur dioxide liquefaction device (397). 5) A carbon dioxide outlet (394) is provided on the lower side of the first internal cavity (396). The first liquid oxygen inlet (393) of the sulfur dioxide liquefaction device (39) is connected to the air-to-liquid oxygen system (43) through a pipeline. The first oxygen outlet (392) is connected to the oxygen storage device (44) through a pipeline. The first gas inlet (391) is connected to the gaseous carbon dioxide storage device (37) through a pipeline. The liquid sulfur dioxide outlet (395) is connected to the liquid sulfur dioxide storage tank (38) through a pipeline. The carbon dioxide outlet (394) is connected to the inlet of the gas compressor station (40) through a pipeline.

3. The clinker production system coupled with cryogenic carbon capture and waste heat power generation according to claim 1, characterized in that: The carbon dioxide liquefaction device (41) consists of a second internal cavity (415) and a second external cavity (416). A second gas inlet (411) is provided at the top and is connected to the second internal cavity (415) through the second external cavity (416). A second liquid oxygen inlet (413) is provided in the middle of the second external cavity (416). A second oxygen outlet (412) is provided at the upper part of the second external cavity (416). A liquid carbon dioxide outlet (414) is provided on the lower side of the second internal cavity (415). The second liquid oxygen inlet (413) of the carbon dioxide liquefaction device (41) is connected to the air-to-liquid oxygen system (43) through a pipeline. The second oxygen outlet (412) is connected to the oxygen storage device (44) through a pipeline. The liquid carbon dioxide outlet (414) is connected to the liquid carbon dioxide storage tank (42) through a pipeline.

4. The clinker production system coupled with cryogenic carbon capture and waste heat power generation according to claim 1, characterized in that: The waste heat power generation boiler (25) is provided with a carbon dioxide working fluid evaporator (251), an economizer (252), an evaporator (253), a steam drum (254), and a superheater (255) in sequence from bottom to top. The economizer (252), evaporator (253), and superheater (255) are respectively connected to the steam drum (254) through pipelines. The superheater (255) is connected to the first steam turbine (27) through pipelines. The first steam turbine (27) is connected to the condenser (26) through pipelines. The condenser (26) is connected to the economizer (252) through pipelines. The carbon dioxide working fluid evaporator (251) is connected to the energy release heat exchanger (28) and the second steam turbine (29) in sequence through pipelines. The waste heat power generation boiler (25) is connected to the liquid carbon dioxide storage tank (42) through pipelines.

5. The clinker production system of all-oxygen combustion coupled with cryogenic carbon capture and waste heat power generation according to claim 1, characterized in that, The cement kiln system includes a preheater (1), a decomposition furnace (2), a smoke chamber (3), a rotary kiln (4), a kiln head hood (5), a grate cooler (6), a first alternative fuel bin (7), a second burner (9), a tertiary air duct (10), a first cooling device (12), a second cooling device (13), a first dust collector (14), a first fan (15), a desulfurization device (16), a denitrification device (17), a kiln feed elevator (18), a humidification tower (19), a first control valve (20), a second control valve (21), a third control valve (22), a fourth control valve (23), a fifth control valve (24), and a high-temperature fan (3). 0); The denitrification device (17) is connected to the upper part of the decomposition furnace (2); The outlet of the desulfurization device (16) is divided into two paths, one path is connected to the pipe between the first cooling device (12) and the second cooling device (13), and the powdered desulfurization material enters the first dust collector (14) through the pipe, and the other path is connected to the kiln elevator (18), and the powdered desulfurization material enters the preheater (1) through the kiln elevator (18); The flue gas outlet pipe at the top of the preheater (1) is divided into two paths and connected to the humidification tower (19) and the waste heat power generation boiler (25) respectively, and the first control valve (20) and the second control valve (21) are respectively installed on the pipe.

6. The clinker production system of all-oxygen combustion coupled with cryogenic carbon capture and waste heat power generation according to claim 1, characterized in that, The raw material grinding system includes a raw material mill (31), a cyclone dust collector (32), a second dust collector (33), a zipper machine (34), and a kiln tail exhaust fan (35); the zipper machine (34) is provided with two inlets that are respectively connected to the outlets of the cyclone dust collector (32) and the second dust collector (33), and the outlet of the zipper machine (34) is connected to the kiln elevator (18).

7. The clinker production system of all-oxygen combustion coupled with cryogenic carbon capture and waste heat power generation according to claim 1, characterized in that, The sulfur dioxide liquefaction device (39) and the carbon dioxide liquefaction device (41) are single devices or a matrix of several devices; the sulfur dioxide liquefaction device (39) further includes a first internal cavity temperature and pressure sensor (398) and a first external cavity temperature and pressure sensor (399); the carbon dioxide liquefaction device (41) further includes a second internal cavity temperature and pressure sensor (417) and a second external cavity temperature and pressure sensor (418).

8. A clinker production method using oxy-fuel combustion coupled with cryogenic carbon capture and waste heat power generation, comprising the clinker production system according to any one of claims 1-7, characterized in that, The following steps are included: S1: In the clinker production process, the raw material grinding system transports the ground raw material to the kiln elevator (18) via a zipper (34), and then into the cement kiln system for calcination to produce cement clinker. The energy required for the calcination process is provided by oxygen and alternative fuels. The oxygen is generated by the liquid oxygen produced by the air-to-liquid oxygen system (43) and then exchanged with the cryogenic carbon capture subsystem. The oxygen enters the oxygen storage device (44) through pipelines, and then is divided into two streams to enter the cement clinker calcination system. The first stream of oxygen enters the first The burner (8) provides 5% to 10% of the energy for cement clinker calcination. The second oxygen supply provides oxygen to the decomposition furnace (2) through the adjustment of the opening of the sixth control valve (45) to assist combustion. The second oxygen supply provides 0% to 5% of the energy for cement clinker calcination. The alternative fuel in the first alternative fuel bin (7) is transported to the second burner (9). The second burner (9) burns the alternative fuel to provide 55% to 60% of the energy for cement clinker calcination. The second alternative fuel bin (11) directly feeds the alternative fuel into the decomposition furnace (2). The energy provided accounts for 40% to 45% of the cement clinker calcination system; the alternative fuel is a mixture of three types: biomass waste fuel, hazardous waste-derived fuel, and hazardous solid waste fuel, with a calorific value between 20 GJ / T and 25 GJ / T; during operation, the operating temperature at the connection between the bottom of the decomposition furnace (2) and the smoke chamber (3) is controlled between 1000℃ and 1100℃, and the outlet temperature at the top of the decomposition furnace (2) is controlled between 880℃ and 890℃; the temperature distribution inside the rotary kiln is as follows: kiln head hood (5) and rotary kiln (4) The temperature at the connection point is controlled between 1600℃ and 1700℃, the temperature in the middle of the rotary kiln (4) is controlled between 1200℃ and 1300℃, and the operating temperature at the connection point between the rotary kiln (4) and the smoke chamber (3) is controlled between 1100℃ and 1200℃. During operation, the temperature of the high-temperature flue gas at the top outlet duct of the preheater (1) is controlled between 250℃ and 350℃. The high-temperature flue gas enters the waste heat power generation boiler (25) under the negative pressure provided by the high-temperature fan (30) to provide heat energy for power generation. S2: Desulfurization and denitrification process. In the S1 clinker production process, the denitrification solution is pumped to the decomposition furnace (2) through the denitrification device (17) and pipeline. In the decomposition furnace (2), it reacts with the material at high temperature to remove nitrogen oxides, which is the denitrification process. The desulfurization powder in the desulfurization device (16) enters the kiln elevator (18) through the pipeline and mixes with the ground raw material before entering the preheater (1). In the preheater (1), it removes sulfides through high temperature reaction. Another desulfurization powder enters the first dust collector (14) through the pipeline and mixes with the material in the first dust collector (14). The high-temperature flue gas after desulfurization and denitrification still contains a small amount of sulfur dioxide, water vapor and dust containing carbon dioxide. S3: Cryogenic carbon capture process. After desulfurization and denitrification in step S2, the high-temperature flue gas is cooled by water spraying from the humidification tower (19) under the negative pressure provided by the high-temperature fan (30) and then enters the raw material mill system. Dust is removed in the second dust collector (33). After dust removal, the high-temperature flue gas only contains a small amount of sulfur dioxide, water vapor and carbon dioxide. The high-temperature flue gas after dust removal enters the cryogenic carbon capture subsystem under the negative pressure provided by the kiln tail exhaust fan (35). In the cryogenic carbon capture subsystem, water vapor is first removed by the condensation tower (36) and then enters the gaseous carbon dioxide storage device. (37) After reaching the specified pressure, it enters the sulfur dioxide liquefaction device (39). In the sulfur dioxide liquefaction device (39), sulfur dioxide is liquefied to form sulfuric acid. The sulfuric acid enters the liquid sulfur dioxide storage tank (38). At this time, the high-temperature flue gas from the kiln tail preheater (1) is reduced to atmospheric carbon dioxide gas. The atmospheric carbon dioxide gas enters the gas compressor station (40) and is compressed into high-pressure carbon dioxide gas. It then enters the carbon dioxide liquefaction device (41) and is liquefied into liquid carbon dioxide. It then enters the liquid carbon dioxide storage tank (42) for storage, thus completing the carbon dioxide capture. S4: The liquid carbon dioxide waste heat power generation process, after the low temperature carbon capture process in step S3, the generated liquid carbon dioxide enters the waste heat power generation system, and is vaporized into high pressure gaseous carbon dioxide in the carbon dioxide working fluid evaporator (251) in the waste heat power generation boiler (25). The high pressure gaseous carbon dioxide then enters the energy release heat exchanger (28), and is heated in the energy release heat exchanger (28) to form high temperature and high pressure gaseous carbon dioxide. The high temperature and high pressure gaseous carbon dioxide enters the second steam turbine (29) to release energy and drive the steam turbine to rotate and drive the electric motor to generate electricity. After releasing energy, the gaseous carbon dioxide becomes normal temperature and pressure carbon dioxide gaseous state and returns to the gaseous carbon dioxide storage device (37) for storage, thus forming a carbon dioxide power generation cycle system. S5: Waste heat power generation process of high-temperature flue gas at the kiln tail. During the clinker production process in S1, when the second control valve (21), the fourth control valve (23), and the fifth control valve (24) are opened simultaneously, the high-temperature flue gas from the kiln tail coming out of the top outlet duct of the preheater (1) enters the waste heat power generation boiler (25). Water enters the waste heat power generation boiler (25) through the economizer (252) and forms superheated steam under the heating of the high-temperature flue gas. The superheated steam then enters the first steam turbine (27) through the pipeline to drive the steam turbine to rotate and generate electricity. At the same time, the superheated steam releases its own cooling capacity and enters the condenser (26) through the first steam turbine (27). It condenses into water inside the condenser (26) and then returns to the waste heat power generation boiler (25) through the pipeline, forming a waste heat power generation cycle system utilizing the high-temperature flue gas at the kiln tail.

9. The clinker production method according to claim 8, which involves oxy-fuel combustion coupled with cryogenic carbon capture and waste heat power generation, is characterized in that: During the S3 cryogenic carbon capture process, by controlling the amount of liquid oxygen supplied and monitoring the temperature and pressure of the temperature and pressure sensor (398) of the first internal cavity of the sulfur dioxide liquefaction device (39) in real time, the temperature inside the first internal cavity (396) is controlled at -10℃ and the pressure is controlled at atmospheric pressure. Under this condition, sulfur dioxide is liquefied and enters the liquid sulfur dioxide storage tank (38), while carbon dioxide continues to remain in a gaseous state and continues to enter the gas compressor station (40).

10. The clinker production method according to claim 8, characterized in that: During the S3 cryogenic carbon capture process, by controlling the amount of liquid oxygen supplied and monitoring the temperature and pressure of the temperature and pressure sensor (417) of the second internal cavity of the carbon dioxide liquefaction device (41) in real time, the temperature inside the second internal cavity (415) is controlled at -50℃ and the pressure is controlled at 0.6MPa. Under this condition, carbon dioxide liquefaction is transported to the liquid carbon dioxide storage tank (42) through pipeline.

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