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WO2025055293A1 - 基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统 - Google Patents

基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统 Download PDF

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Publication number
WO2025055293A1
WO2025055293A1 PCT/CN2024/082048 CN2024082048W WO2025055293A1 WO 2025055293 A1 WO2025055293 A1 WO 2025055293A1 CN 2024082048 W CN2024082048 W CN 2024082048W WO 2025055293 A1 WO2025055293 A1 WO 2025055293A1
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WO
WIPO (PCT)
Prior art keywords
fan
carbon dioxide
heat exchange
flue gas
speed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/CN2024/082048
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English (en)
French (fr)
Inventor
张超
王彬
张思才
马爱国
陶瑛
迟大亮
张婉君
郑现明
邓玉华
姚秀丽
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
CBMI CONSTRUCTION Co Ltd
CBMI Construction Co Ltd
Original Assignee
CBMI CONSTRUCTION Co Ltd
CBMI Construction Co Ltd
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Filing date
Publication date
Application filed by CBMI CONSTRUCTION Co Ltd, CBMI Construction Co Ltd filed Critical CBMI CONSTRUCTION Co Ltd
Publication of WO2025055293A1 publication Critical patent/WO2025055293A1/zh
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories or equipment specially adapted for rotary-drum furnaces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories or equipment specially adapted for rotary-drum furnaces
    • F27B7/34—Arrangements of heating devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories or equipment specially adapted for rotary-drum furnaces
    • F27B7/38—Arrangements of cooling devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories or equipment specially adapted for rotary-drum furnaces
    • F27B7/42—Arrangement of controlling, monitoring, alarm or like devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases

Definitions

  • the present disclosure relates to the technical field of cement calcination, and in particular to a method and system for obtaining high-concentration carbon dioxide flue gas based on calcining cement clinker.
  • the carbon dioxide capture system is used to remove carbon dioxide from the gas stream or separate carbon dioxide as a gas product. Capture is the first step of carbon capture and storage (CCS technology). Carbon dioxide needs to be present in a high purity during transportation and storage, and in most cases the concentration of carbon dioxide in industrial exhaust gas does not meet this requirement, so carbon dioxide must be separated from the exhaust gas. This process is called carbon dioxide capture. Carbon dioxide capture systems can be divided into several categories, such as chemical absorption, physical absorption, physical adsorption, membrane separation, and cryogenic separation. When applied, the capture method and equipment must be selected based on the actual characteristics and parameters of the carbon dioxide emission source.
  • the embodiments of the present disclosure provide a method and system for obtaining high-concentration carbon dioxide flue gas based on calcining cement clinker, which can obtain high-concentration carbon dioxide flue gas with low energy consumption.
  • the present disclosure provides a system for obtaining high-concentration carbon dioxide flue gas based on calcining cement clinker, comprising: a rotary kiln, a smoke chamber and a kiln head cover are respectively arranged at the tail and the head of the rotary kiln, and the rotary kiln surrounds an electromagnetic induction device along the length direction; a pressure sensor and a gas analyzer are arranged in the kiln head cover;
  • the air cooling device being connected to the kiln head cover and used for cooling the clinker produced by the rotary kiln heating and calcining the raw material via the electromagnetic induction device by air, the kiln head cover being provided with a hot air duct for guiding out the air after the heat exchange;
  • a first heat exchange device connected to the smoke chamber, used for heat exchange between raw meal and smoke generated by calcining the raw meal in the rotary kiln, the first heat exchange device comprising a first raw meal inlet for introducing raw meal and a first raw meal outlet for leading the raw meal after heat exchange to the smoke chamber;
  • a second heat exchange device connected to the smoke chamber and the hot air duct respectively, used for exchanging heat between the raw meal and the air after heat exchange, the second heat exchange device comprising a second raw meal inlet for introducing the raw meal and a second raw meal outlet for leading the raw meal after heat exchange to the smoke chamber;
  • a flue gas duct connected to the first heat exchange device, wherein the flue gas duct is provided with a first fan for discharging the flue gas after heat exchange;
  • a control device the control device is respectively connected to the pressure sensor, the gas analyzer, the first fan and the second fan, and the control device is used to: when the carbon dioxide concentration monitored by the gas analyzer is greater than a threshold value, control the rotation speed of the first fan to gradually increase until it stays at a rotation speed that can reduce the carbon dioxide concentration to the threshold value, during which the pressure value monitored by the pressure sensor is within a preset range value; if in the process of controlling the rotation speed of the first fan to gradually increase, the pressure value monitored by the pressure sensor is greater than the upper limit of the preset range value, control the rotation speed of the second fan to gradually decrease, at this time the rotation speed of the first fan remains unchanged, until the first fan and the second fan remain at a rotation speed that can reduce the carbon dioxide concentration to the threshold value and the pressure value to the preset range value; if in the process of controlling the rotation speed of the second fan to gradually decrease, the carbon dioxide concentration has not yet dropped to the threshold when the pressure value monitored by the pressure sensor is less than the lower limit of the preset range value
  • the raw material in the rotary kiln is heated and calcined by an electromagnetic induction device, and the raw material decomposes to release carbon dioxide gas.
  • the rotation speed of the first fan and the second fan is regulated by the control device to control the carbon dioxide concentration to a threshold value and the pressure value to a preset range value, so that the carbon dioxide flue gas and the air after heat exchange each take their own paths and do not mix, thereby further ensuring a high concentration of carbon dioxide;
  • the entire system uses air to cool the clinker, and uses the carbon dioxide flue gas and the air after heat exchange to preheat the raw material, so that energy is reused and energy consumption is low.
  • the first heat exchange device comprises a plurality of cyclones arranged from top to bottom, the bottom material outlet of the lowest cyclone is connected to the smoke chamber, the gas inlet of the lowest cyclone is connected to the smoke chamber, and the top gas outlet of the highest cyclone is connected to the smoke duct; wherein the gas outlet of the lower cyclone is connected to the upper cyclone through a connecting duct, and the bottom material outlet of the upper cyclone is connected to the lower connecting duct;
  • the raw material is fed into the connecting pipe located at the top.
  • the second heat exchange device also includes a plurality of cyclone barrels arranged from top to bottom, the bottom material outlet of the cyclone barrel located at the bottom is connected to the smoke chamber, the gas inlet of the cyclone barrel located at the bottom is connected to the hot air duct, and the top gas outlet of the cyclone barrel located at the top is connected to the air duct; wherein the gas outlet of the cyclone barrel located at the bottom is connected to the cyclone barrel located at the top through a connecting pipe, and the bottom material outlet of the cyclone barrel located at the top is connected to the connecting pipe at the bottom;
  • the raw material is fed into the connecting pipe located at the top.
  • the wind cooling device includes a grate cooler, and a blower for introducing air is arranged at the bottom of the grate cooler.
  • the ratio of raw materials fed into the first heat exchange device and the second heat exchange device is 1:(2-5).
  • the flue gas discharged from the flue gas duct is further processed by a dust collector, and the processed flue gas can be connected to a carbon dioxide capture system.
  • the flue gas duct and/or the air duct is also connected to a waste heat boiler.
  • the present disclosure further provides a method for obtaining high-concentration carbon dioxide flue gas based on calcining cement clinker.
  • the system based on the above technical solution specifically comprises the following steps:
  • the raw material is heated and decomposed in a rotary kiln equipped with an electromagnetic induction device to produce carbon dioxide gas, while being calcined into clinker;
  • the flue gas containing the carbon dioxide gas generated by decomposition enters the first heat exchange device through the smoke chamber, and the clinker passes through the kiln head
  • the hood enters the air cooling device to exchange heat with the air for cooling, and the air after heat exchange enters the second heat exchange device;
  • the raw material Before entering the rotary kiln, the raw material is put into the first heat exchange device and the second heat exchange device respectively to exchange heat with the flue gas and air. After the heat exchange, the raw material enters the rotary kiln through the smoke chamber for calcination.
  • the flue gas and air after the heat exchange are discharged through the flue gas duct and the air duct respectively; wherein, the flue gas discharged through the flue gas duct is a high-concentration carbon dioxide flue gas, and the carbon dioxide concentration in the flue gas is greater than 80%;
  • the first fan when the carbon dioxide concentration monitored by the gas analyzer is greater than the threshold value, gradually increases the speed until it stays at the speed when the carbon dioxide concentration drops to the threshold value, and the pressure value monitored by the pressure sensor during this period is always within the preset range value; in the above process, if the pressure value monitored by the pressure sensor is greater than the upper limit of the preset range value but the carbon dioxide concentration has not dropped to the threshold value while the first fan is gradually increasing the speed, the second fan begins to gradually reduce the speed, while the first fan maintains the speed unchanged, until the first fan and the second fan respectively stay at the speeds when the carbon dioxide concentration drops to the threshold value and the pressure value drops to the preset range value; in the above process, if the second fan is gradually reducing the speed, the carbon dioxide concentration still does not drop to the threshold when the pressure value is less than the lower limit of the preset range value, the first fan continues to gradually increase the speed, while the second fan maintains the speed unchanged; repeat the above steps until the first fan and the second fan stay at the speeds when the carbon
  • the beneficial effects that can be obtained are at least:
  • the raw material in the rotary kiln is heated and calcined by an electromagnetic induction device, and the raw material decomposes to release carbon dioxide gas.
  • no air is introduced, no flue gas is generated from the combustion of fuel, the amount of waste gas is greatly reduced, and the carbon dioxide concentration in the generated carbon dioxide flue gas is high;
  • the rotation speed of the first fan and the second fan is regulated by the control device, and the carbon dioxide concentration is controlled to drop to a threshold value and the pressure value to drop to a preset range value, so as to prevent the carbon dioxide gas released by the decomposition of the raw material in the rotary kiln from mixing with the air after heat exchange, thereby further ensuring a high concentration of carbon dioxide.
  • FIG1 is an overall schematic diagram of a system for obtaining high-concentration carbon dioxide flue gas based on calcining cement clinker according to an embodiment of the present disclosure.
  • FIG. 2 is a schematic diagram showing the connection between a control device and a pressure sensor, a gas analyzer, a first fan and a second fan in a system for obtaining high-concentration carbon dioxide flue gas based on calcining cement clinker according to an embodiment of the present disclosure.
  • the present disclosure provides a system 100 for obtaining high-concentration carbon dioxide flue gas based on calcining cement clinker, which is applied in the field of cement calcining technology to solve the problem of low carbon dioxide concentration in flue gas generated by existing cement calcining processes.
  • the system 100 includes a rotary kiln 110, an air cooling device, a first heat exchange device 130, a second heat exchange device 140, a flue gas duct 150, an air duct 160, and a control device 170.
  • the rotary kiln 110 is used to heat and calcine raw materials.
  • the air cooling device is used to air-cool the clinker generated by calcining the raw materials.
  • the first heat exchange device 130 is used to preheat the raw materials fed into the rotary kiln 110 with flue gas.
  • the second heat exchange device 140 is used to preheat the raw materials fed into the rotary kiln 110 with air.
  • the flue gas duct 150 is used to discharge the flue gas generated by the rotary kiln 110 to obtain high-concentration carbon dioxide flue gas.
  • the air duct 160 is used to discharge the air after heat exchange.
  • the control device 170 is used to control the pressure balance in the kiln head hood 112 so that the carbon dioxide flue gas generated in the rotary kiln 110 and the air passing through the kiln head hood 112 are not mixed to ensure a high concentration of carbon dioxide in the flue gas.
  • a smoke chamber 111 and a kiln head cover 112 are respectively provided at the tail and head of the rotary kiln 110.
  • the raw material enters the rotary kiln 110 through the smoke chamber 111.
  • the smoke is discharged outward through the smoke chamber 111.
  • the clinker is guided outward through the kiln head cover 112.
  • the rotary kiln 110 is a rotatable cylindrical structure.
  • the rotary kiln 110 may include an inlet section, a sintering section, and a cooling section.
  • the rotary kiln 110 surrounds an electromagnetic induction device 113 along the length direction, for example, an electromagnetic induction coil.
  • High-frequency alternating current generates an alternating magnetic field through the coil, causing the rotary kiln 110 to generate eddy current self-heating.
  • the raw material in the rotary kiln 110 is heated to decompose carbonates, and the decomposition product CaO of the raw material during the process of moving diffuses with SiO 2 , Fe 2 O 3 , Al 2 O 3 and the like in the raw material to react in a solid phase to form clinker minerals. In this process, carbonates decompose to produce carbon dioxide.
  • a pressure sensor 114 and a gas analyzer 115 are provided in the kiln head hood 112.
  • the pressure sensor 114 is used to monitor the pressure data in the kiln head hood 112 in real time.
  • the gas analyzer 115 is used to monitor the carbon dioxide concentration in the kiln head hood 112 in real time, and to understand whether the air in the kiln head hood 112 is mixed with smoke by monitoring whether the carbon dioxide concentration exceeds the normal carbon dioxide content in the air (the carbon dioxide content in the air is 0.03%).
  • the air cooling device is connected to the kiln head cover 112.
  • the air cooling device is used to use air to cool the clinker produced by heating and calcining raw materials in the rotary kiln 110 via the electromagnetic induction device 113.
  • the kiln head cover 112 is configured to conduct air after heat exchange.
  • the air cooling device may be a prior art device.
  • the air cooling device may be a grate cooler 120.
  • a blower 121 for introducing air may be provided at the bottom of the grate cooler 120.
  • the cooling gas in this embodiment may be air, or other cooling gases may be used, and the gas object monitored by the gas analyzer 115 may be adaptively adjusted accordingly.
  • the first heat exchange device 130 is connected to the smoke chamber 111.
  • the first heat exchange device 130 is used for heat exchange between raw materials and smoke generated by calcining raw materials in the rotary kiln 110.
  • the first heat exchange device 130 includes a first raw material inlet for introducing raw materials and a first raw material outlet for leading the raw materials after heat exchange to the smoke chamber 111.
  • the first heat exchange device 130 can be a prior art device.
  • the second heat exchange device 140 is connected to the smoke chamber 111 and the hot air duct 122 respectively.
  • the second heat exchange device 140 is used for heat exchange between the raw material and the air after heat exchange.
  • the second heat exchange device 140 includes a second raw material inlet for introducing the raw material and a second raw material outlet for leading the raw material after heat exchange to the smoke chamber 111.
  • the second heat exchange device 140 can be a prior art device.
  • the flue gas duct 150 is connected to the first heat exchange device 130.
  • the flue gas duct 150 is equipped with a first fan 151 for discharging the flue gas after heat exchange. Under normal circumstances, the first fan 151 operates at a certain speed.
  • the air duct 160 is connected to the second heat exchange device 140.
  • the air duct 160 is equipped with a second fan 161 for discharging the air after the secondary heat exchange. Under normal circumstances, the second fan 161 operates at a certain speed.
  • the control device 170 is connected to the pressure sensor 114, the gas analyzer 115, the first fan 151 and the second fan 161 respectively.
  • the control device 170 controls the rotation speed of the first fan 151 to gradually increase until it stays at the rotation speed when the carbon dioxide concentration drops to the threshold value, during which the pressure value monitored by the pressure sensor 114 is within the preset range, for example, between negative 10Pa and negative 35Pa.
  • the control device 170 controls the rotation speed of the second fan 161 to gradually decrease, and the rotation speed of the first fan 151 remains unchanged (i.e., the rotation speed when the second fan 161 starts to be adjusted) until the first fan 151 and the second fan 161 stay at the rotation speed when the carbon dioxide concentration drops to the threshold value and the pressure value drops to the preset range.
  • the control device 170 controls the speed of the first fan 151 to continue to increase gradually, and the speed of the second fan 161 remains unchanged (i.e., the speed at which the speed of the first fan 151 is adjusted is maintained). The above process is repeated until the first fan 151 and the second fan 161 stay at the speed at which the carbon dioxide concentration drops to the threshold value and the pressure value drops to within the preset range value.
  • control device 170 cooperates with the pressure sensor 114, the gas analyzer 115, and the first fan 151
  • the adjustment made with the second fan 161 is aimed at achieving a pressure balance point in the rotary kiln 110 at the kiln outlet end (near the kiln head hood 112), so that the carbon dioxide gas generated by the thermal decomposition of the raw materials in the rotary kiln 110 is discharged only through the rotary kiln 110, the smoke chamber 111 and the first heat exchange device 130, and the air that exchanges heat with the clinker passes through the kiln head hood 112 and is discharged only through the hot air duct 122 and the second heat exchange device 140, and the two are not mixed, thereby ensuring a high concentration of carbon dioxide in the flue gas.
  • the first heat exchange device 130 may include a plurality of cyclones 180 arranged from top to bottom.
  • the number of cyclones 180 may not be limited, for example, it may be 5, 6 or other numbers.
  • the bottom material outlet of the cyclone 180 located at the bottom is connected to the smoke chamber 111.
  • the gas inlet of the cyclone 180 located at the bottom is connected to the smoke chamber 111.
  • the top gas outlet of the cyclone 180 located at the top is connected to the flue gas duct 150.
  • the gas outlet of the cyclone 180 located at the bottom is connected to the cyclone 180 located at the top through the connecting pipe 181.
  • the bottom material outlet of the cyclone 180 located at the top is connected to the connecting pipe 181 at the bottom.
  • the raw material is put into the connecting pipe 181 located at the top.
  • the second heat exchange device 140 may also include a plurality of cyclones 180 arranged from top to bottom.
  • the number of cyclones 180 may not be limited, for example, it may be 5, 6 or other numbers.
  • the bottom material outlet of the cyclone 180 located at the bottom is connected to the smoke chamber 111.
  • the gas inlet of the cyclone 180 located at the bottom is connected to the hot air duct 122.
  • the top gas outlet of the cyclone 180 located at the top is connected to the air duct 160.
  • the gas outlet of the cyclone 180 located at the bottom is connected to the cyclone 180 located at the top through the connecting duct 181.
  • the bottom material outlet of the cyclone 180 located at the top is connected to the connecting duct 181 at the bottom.
  • the raw material is put into the connecting duct 181 located at the top.
  • the ratio of raw materials fed into the first heat exchanger 130 and the second heat exchanger 140 is 1:(2-5). For example, about 1/4 of the raw materials are fed into the first heat exchanger 130, and about 3/4 of the raw materials are fed into the second heat exchanger 140.
  • the raw meal is fed from the connecting pipe 181 between the cyclone C2A and C1-A1, C1-A2, and the connecting pipe 181 between C2B and C1-B1, C1-B2 of the first heat exchange device 130. About 1/4 of the raw meal is fed into the connecting pipe 181 between C2A and C1-A1, C1-A2, and 3/4 of the raw meal is fed into the connecting pipe 181 between C2B and C1-B1, C1-B2.
  • the raw meal is dispersed and heat-exchanged in the connecting pipe 181, and enters the cyclone C1-A1, C1-A2, C1-B1, C1-B2 with the air flow.
  • the raw meal is separated in the cyclone 180, and the gas is discharged from the top of the cyclone 180.
  • the cyclone C1-A1 and C1-A2 discharges high-concentration carbon dioxide flue gas, and the cyclone C1-B1 and C1-B2 discharges hot air.
  • the raw meal is collected in the cone of the cyclone 180 and discharged.
  • the raw meal discharged from the cone of C1-A1 and C1-A2 cyclones is fed into the connecting pipe 181 between C2A and C3A; the raw meal discharged from the cone of C1-B1 and C1-B2 cyclones is fed into the connecting pipe 181 between C2B and C3B.
  • the raw meal is dispersed and heat-exchanged in the connecting pipe 181, and enters the C2A and C2B cyclones with the airflow.
  • the material gas is separated in the cyclone 180, and the gas is discharged from the top of the cyclone 180.
  • the C2A cyclone discharges high-concentration carbon dioxide flue gas
  • the C2B cyclone discharges hot air.
  • the raw meal is collected in the cone of C2A and C2B cyclones and discharged. Similarly, the materials pass through the C3A, C3B, C4A, C4B, C5A, C5B, C6A, C6B cyclones, and the raw meal after heating is finally discharged from the cone of C6A and C6B cyclones and fed into the smoke chamber 111.
  • the raw material After heating, the raw material is fed into the smoke chamber 111 and then enters the rotary kiln 110.
  • the high-frequency alternating current generates an alternating magnetic field through the coil, causing the rotary kiln 110 to generate eddy current self-heating.
  • the raw material is heated in the kiln to decompose carbonates.
  • the decomposition product CaO of the material during the process diffuses with SiO 2 , Fe 2 O 3 , Al 2 O 3 and the like in the raw material to react in the solid phase to form clinker minerals.
  • the material passes through the kiln, completing the above clinker calcination process.
  • the carbon dioxide gas generated by the decomposition of carbonates is transported from the kiln and the kiln tail smoke chamber 111 to the inlet of the cyclone C6A.
  • the calcined clinker is fed into the front section of the grate cooler 120.
  • the clinker moves continuously from the inlet to the outlet on the grate cooler 120, and at the same time exchanges heat with the air entering from the blower 121 at the bottom of the grate cooler 120, completing the cooling of the clinker and heat recovery.
  • the high-temperature hot air of 700-850 degrees enters the inlet of the cyclone C6B through the kiln head cover 112 and the hot air duct 122.
  • the pressure balance point in the kiln is located at the kiln outlet.
  • the end (close to the kiln head cover 112) is used to realize that the CO2 decomposed in the kiln only goes through the rotary kiln 110 and enters the kiln tail smoke chamber 111, and the high-temperature hot air only enters the hot air duct 122 through the kiln head cover 112, so that the two gases each go their own way and do not mix.
  • Excess preheat at the tail end of the grate cooler 120 is discharged from the tail end and can enter the waste heat boiler 190 or be used for drying materials, etc.
  • the present disclosure also provides a method for obtaining high-concentration carbon dioxide flue gas based on calcining cement clinker, and a system 100 based on the above technical solution.
  • the method specifically comprises the following steps:
  • the flue gas containing the decomposed carbon dioxide gas enters the first heat exchange device 130 through the smoke chamber 111.
  • the clinker enters the air cooling device through the kiln head cover 112 to exchange heat with the air for cooling, and the air after heat exchange enters the second heat exchange device 140.
  • the raw material Before entering the rotary kiln 110, the raw material is respectively put into the first heat exchange device 130 and the second heat exchange device 140 for heat exchange with flue gas and air. After heat exchange, the raw material enters the rotary kiln 110 through the smoke chamber 111 for calcination.
  • the flue gas and air after heat exchange are discharged through the flue gas duct 150 and the air duct 160 respectively; wherein, the flue gas discharged through the flue gas duct 150 is high-concentration carbon dioxide flue gas, and the carbon dioxide concentration in the flue gas is greater than 80%.
  • the first fan 151 when the carbon dioxide concentration monitored by the gas analyzer 115 is greater than the threshold value, the first fan 151 gradually increases the speed until it stays at the speed when the carbon dioxide concentration drops to the threshold value, and the pressure value monitored by the pressure sensor 114 is always within the preset range value during the process; in the above process, if the pressure value monitored by the pressure sensor 114 is greater than the upper limit of the preset range value but the carbon dioxide concentration has not dropped to the threshold value during the process of gradually increasing the speed of the first fan 151, the second fan 161 begins to gradually reduce the speed, while the first fan 151 keeps the speed unchanged, until the first fan 151 and the second fan 161 respectively stay at the speed when the carbon dioxide concentration drops to the threshold value and the pressure value drops to the preset range value; in the above process, if the second fan 161 is in the process of gradually reducing the speed, the carbon dioxide concentration still does not drop to the threshold value when the pressure value is less than the lower limit of the preset range value, the first fan 151 continues to gradually increase the

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Abstract

本公开提供一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统，其中系统包括：回转窑设置烟室和窑头罩，回转窑沿长度方向环绕电磁感应装置；窑头罩内设置压力传感器和气体分析仪；风冷却装置用于利用空气冷却回转窑经由电磁感应装置加热煅烧生料所产生的熟料；第一换热装置用于生料和回转窑煅烧生料所产生的烟气进行换热；第二换热装置用于生料和经过换热后的空气进行换热；烟气管道安装第一风机，用于将经过换热后的烟气排出；空气管道安装第二风机，用于将经过二次换热后的空气排出；控制装置用于调控第一风机和第二风机的转速，使二氧化碳浓度降至阈值和压力值降至预设范围值内。根据本公开提供的系统，可以获得高浓度二氧化碳烟气。

Description

基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统
相关申请
本公开要求于2023年09月15日提交中国专利局、申请号为CN202311194724.X、发明名称为“基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本公开涉及水泥煅烧技术领域，尤其涉及一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统。
背景技术
二氧化碳捕获系统用于去除气流中的二氧化碳或者分离出二氧化碳作为气体产物。捕获是碳捕获与封存(carbon capture and storage，简称CCS技术)的第一步。二氧化碳在运输和封存时需要以较高的纯度存在，而在大多数情况下工业尾气中二氧化碳的浓度达不到这个要求，所以必须从尾气中将二氧化碳分离出来，这一过程称为二氧化碳的捕获。二氧化碳捕获系统可以分为化学吸收、物理吸收、物理吸附、膜分离、深冷分离等若干类别，在应用时需要根据二氧化碳排放源的实际特点和参数等进行捕获方式和设备的选择。
在实现本公开过程中，发明人发现现有技术中至少存在如下问题：
常规的回转窑水泥煅烧工艺需要有燃料燃烧，助燃介质为空气，最终产生的烟气中二氧化碳的浓度较低，一般在18-25％之间。而二氧化碳捕获系统的投资与运行成本与二氧化碳浓度有很大关系，常规的回转窑水泥煅烧工艺产生的低浓度的二氧化碳烟气将大大增加二氧化碳捕获系统的投资与运行成本。
因此需要一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统，以至少部分地解决上述技术问题。
发明内容
本公开实施例提供了一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统，可以获得高浓度二氧化碳烟气，能耗低。
第一方面，本公开提供一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的系统，包括：回转窑，所述回转窑的尾部和头部分别设置烟室和窑头罩，所述回转窑沿长度方向环绕电磁感应装置；所述窑头罩内设置压力传感器和气体分析仪；
风冷却装置，所述风冷却装置连通至所述窑头罩，用于利用空气冷却所述回转窑经由所述电磁感应装置加热煅烧生料所产生的熟料，所述窑头罩设置用于导出经过换热后的空气的热风管道；
连通至所述烟室的第一换热装置，用于生料和所述回转窑煅烧生料所产生的烟气进行换热，所述第一换热装置包括用于引入生料的第一生料入口和用于将经过换热后的生料引出至所述烟室的第一生料出口；
分别连通至所述烟室和所述热风管道的第二换热装置，用于生料和所述经过换热后的空气进行换热，所述第二换热装置包括用于引入生料的第二生料入口和用于将经过换热后的生料引出至所述烟室的第二生料出口；
连通至所述第一换热装置的烟气管道，所述烟气管道安装第一风机，用于将经过换热后的烟气排出；
连通至所述第二换热装置的空气管道，所述空气管道安装第二风机，用于将经过二次换热后的空气排出；
控制装置，所述控制装置分别连接至所述压力传感器、所述气体分析仪、所述第一风机和所述第二风机，所述控制装置用于：当所述气体分析仪监测的二氧化碳浓度大于阈值时，控制所述第一风机的转速逐步提高，直至停留在能使二氧化碳浓度降至阈值时的转速，期间所述压力传感器监测的压力值处于预设范围值内；若控制所述第一风机的转速逐步提高的过程中，所述压力传感器监测的压力值大于预设范围值上限，控制所述第二风机的转速逐步降低，此时所述第一风机的转速不变，直至所述第一风机、所述第二风机停留在能使二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速；若控制所述第二风机的转速逐步降低的过程中，所述压力传感器监测的压力值小于预设范围值下限时二氧化碳浓度仍未降至阈值，控制所述第一风机的转速继续逐步提高，此时所述第二风机的转速不变；重复上述过程，直至所述第一风机、所述第二风机停留在能使二 氧化碳浓度降至阈值和压力值降至预设范围值内时的转速。
根据本公开的系统，通过电磁感应装置对回转窑内的生料加热煅烧，生料分解释放二氧化碳气体，相较于传统的通过燃料燃烧方式，不带入空气，产生的二氧化碳烟气中二氧化碳浓度高；同时，通过控制装置调控第一风机和第二风机的转速，控制二氧化碳浓度降至阈值和压力值降至预设范围值内，以使二氧化碳烟气和换热后的空气各自走各自的路径，不混合，进一步确保二氧化碳的高浓度；另外，整个系统利用空气对熟料降温，又利用二氧化碳烟气、换热后的空气对生料预热，能量重复利用，能耗低。
可选地，所述第一换热装置包括从上往下布置的多个旋风筒，位于最下方的旋风筒的底部物料出口连通至所述烟室，位于最下方的旋风筒的气体入口连通至所述烟室，位于最上方的旋风筒的顶部气体出口连通至所述烟气管道；其中，位于下方的旋风筒的气体出口通过连接管道连通至位于上方的旋风筒，位于上方的旋风筒的底部物料出口连通至下方的所述连接管道；
其中，生料投入至位于最上方的所述连接管道。
可选地，所述第二换热装置也包括从上往下布置的多个旋风筒，位于最下方的旋风筒的底部物料出口连通至所述烟室，位于最下方的旋风筒的气体入口连通至所述热风管道，位于最上方的旋风筒的顶部气体出口连通至所述空气管道；其中，位于下方的旋风筒的气体出口通过连接管道连通至位于上方的旋风筒，位于上方的旋风筒的底部物料出口连通至下方的所述连接管道；
其中，生料投入至位于最上方的所述连接管道。
可选地，所述风冷却装置包括篦冷机，所述篦冷机的底部设置用于引入空气的鼓风机。
可选地，投入所述第一换热装置和所述第二换热装置的生料的比例为1∶(2-5)。
可选地，所述烟气管道排出的烟气还经由收尘器处理，处理后的烟气可连通至二氧化碳捕获系统。
可选地，所述烟气管道和/或所述空气管道还连接至余热锅炉。
第二方面，本公开还提供一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法，基于上述技术方案的系统，具体包括以下步骤：
生料在设置电磁感应装置的回转窑内受热分解产生二氧化碳气体，同时煅烧成熟料；
包含所分解产生的二氧化碳气体的烟气经由烟室进入第一换热装置，熟料经由窑头 罩进入风冷却装置与空气换热进行降温，换热后的空气进入第二换热装置；
生料在进入回转窑之前，分别投入第一换热装置和第二换热装置中与烟气和空气换热，换热后通过烟室进入回转窑煅烧，换热后的烟气和空气分别通过烟气管道和空气管道排出；其中，通过烟气管道排出的烟气为高浓度二氧化碳烟气，烟气中二氧化碳浓度大于80％；
其中，当气体分析仪监测的二氧化碳浓度大于阈值时，第一风机逐步提高转速，直至停留在二氧化碳浓度降至阈值时的转速，且期间压力传感器监测的压力值一直处于预设范围值内；上述过程中，若第一风机在逐步提高转速的过程中，压力传感器监测的压力值大于预设范围值上限但二氧化碳浓度未降至阈值，则第二风机开始逐步降低转速，而第一风机保持转速不变，直至第一风机、第二风机分别停留在二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速；上述过程中，若第二风机在逐步降低转速的过程中，压力值小于预设范围值下限时二氧化碳浓度仍未降至阈值，第一风机又继续逐步提高转速，而第二风机保持转速不变；重复上述步骤，直至第一风机、第二风机停留在二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速。
通过利用根据本公开实施例的技术方案，可以获得的有益效果至少在于：
1、通过电磁感应装置对回转窑内的生料加热煅烧，生料分解释放二氧化碳气体，相较于传统的通过燃料燃烧方式，不带入空气，没有来自燃烧燃料产生的烟气，废气量大幅度降低，产生的二氧化碳烟气中二氧化碳浓度高；
2、通过设置的控制装置、压力传感器和气体分析仪，通过控制装置调控第一风机和第二风机的转速，控制二氧化碳浓度降至阈值和压力值降至预设范围值内，目的在于使回转窑内生料分解释放的二氧化碳气体，与换热后的空气不混合，进一步确保二氧化碳的高浓度。
本公开的附加优点、目的，以及特征将在下面的描述中将部分地加以阐述，且将对于本领域普通技术人员在研究下文后部分地变得明显，或者可以根据本公开的实践而获知。本公开的目的和其它优点可以通过在说明书以及附图中具体指出的结构实现到并获得。
本领域技术人员将会理解的是，能够用本公开实现的目的和优点不限于以上具体所述，并且根据以下详细说明将更清楚地理解本公开能够实现的上述和其他目的。
附图说明
此处所说明的附图用来提供对本公开的进一步理解，构成本公开的一部分，并不构成对本公开的限定。附图中的部件不是成比例绘制的，而只是为了示出本公开的原理。为了便于示出和描述本公开的一些部分，附图中对应部分可能被放大，即，相对于依据本公开实际制造的示例性装置中的其它部件可能变得更大。在附图中：
图1为本公开一实施例的基于煅烧水泥熟料获得高浓度二氧化碳烟气的系统的整体示意图；以及
图2为本公开一实施例的基于煅烧水泥熟料获得高浓度二氧化碳烟气的系统中的控制装置分别与压力传感器、气体分析仪、第一风机和第二风机的连接示意图。
附图标记说明：
100、系统；
110、回转窑；111、烟室；112、窑头罩；113、电磁感应装置；114、压力传感器；
115、气体分析仪；
120、篦冷机；121、鼓风机；122、热风管道；
130、第一换热装置；
140、第二换热装置；
150、烟气管道；151、第一风机；
160、空气管道；161、第二风机；
170、控制装置；
180、旋风筒；181、连接管道；
190、余热锅炉；191、收尘器；192、二氧化碳捕获系统。
具体实施方式
通过参考示范性实施例，本公开的目的和功能以及用于实现这些目的和功能的方法将得以阐明。然而，本公开并不受限于以下所公开的示范性实施例；可以通过不同形式来对其加以实现。说明书的实质仅仅是帮助相关领域技术人员综合理解本公开的具体细节。
应予以注意的是，这里所使用的术语仅是为了描述具体实施方式，而非意图限制根据本公开的示例性实施方式。如在这里所使用的，除非上下文另外明确指出，否则单数形式也意图包括复数形式。此外，还应当理解的是，当在本说明书中使用术语“包含”和/或“包括”时，其指明存在特征、整体、步骤、操作、元件和/或组件，但不排除 存在或附加一个或多个其他特征、整体、步骤、操作、元件、组件和/或它们的组合。
本公开中所引用的诸如“第一”和“第二”的序数词仅仅是标识，而不具有任何其他含义，例如特定的顺序等。而且，例如，术语“第一部件”其本身不暗示“第二部件”的存在，术语“第二部件”本身不暗示“第一部件”的存在。
需要说明的是，本文中所使用的术语“上”、“下”、“前”、“后”、“左”、“右”、“内”、“外”以及类似的表述只是为了说明的目的，并非限制。
第一方面，本公开提供一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的系统100，应用于水泥煅烧技术领域，解决现有的水泥煅烧工艺产生的烟气二氧化碳浓度低的问题。
如图1和图2所示，在优选实施例中，系统100包括回转窑110、风冷却装置、第一换热装置130、第二换热装置140、烟气管道150、空气管道160和控制装置170。回转窑110用于加热煅烧生料。风冷却装置用于对煅烧生料生成的熟料进行风冷。第一换热装置130用于对投入回转窑110的生料利用烟气进行预热。第二换热装置140用于对投入回转窑110的生料利用空气进行预热。烟气管道150用于排出回转窑110产生的烟气，获得高浓度二氧化碳烟气。空气管道160用于排出换热后的空气。控制装置170用于控制窑头罩112内的压力平衡，使回转窑110内产生的二氧化碳烟气与窑头罩112内通过的空气不混合，以保证烟气中二氧化碳的高浓度。
具体地，回转窑110的尾部和头部分别设置烟室111和窑头罩112。生料通过烟室111进入回转窑110。烟气通过烟室111向外排出。熟料通过窑头罩112向外导出。回转窑110为可旋转的筒体结构。回转窑110可以包括进口段、烧成段和冷却段。回转窑110沿长度方向环绕电磁感应装置113，例如采用电磁感应线圈。高频交流电通过线圈产生交变磁场，使回转窑110产生涡流自发热。在回转窑110内生料经过加热实现碳酸盐分解,生料在行进过程中的分解产物CaO与生料中的SiO2、Fe2O3、Al2O3等相互扩散进行固相反应，形成熟料矿物。在此过程中碳酸盐分解产生二氧化碳。
窑头罩112内设置压力传感器114和气体分析仪115。压力传感器114用于实时监测窑头罩112内的压力数据。气体分析仪115用于实时监测窑头罩112内的二氧化碳浓度，通过监测二氧化碳浓度是否超过空气中的二氧化碳正常含量(空气中二氧化碳含量为0.03％)，以了解窑头罩112内的空气是否有烟气混合。
风冷却装置连通至窑头罩112。风冷却装置用于利用空气冷却回转窑110内经由电磁感应装置113加热煅烧生料所产生的熟料。窑头罩112设置用于导出经过换热后的空 气的热风管道122。其中，风冷却装置可以是现有技术装置。例如，风冷却装置可以采用篦冷机120。篦冷机120的底部可以设置用于引入空气的鼓风机121。本实施例中的冷却气体采用空气，也可以采用其他冷却气体，相应地气体分析仪115监测的气体对象适应性调整。
第一换热装置130连通至烟室111。第一换热装置130用于生料和回转窑110煅烧生料所产生的烟气进行换热。第一换热装置130包括用于引入生料的第一生料入口和用于将经过换热后的生料引出至烟室111的第一生料出口。其中，第一换热装置130可以是现有技术装置。
第二换热装置140分别连通至烟室111和热风管道122。第二换热装置140用于生料和经过换热后的空气进行换热。第二换热装置140包括用于引入生料的第二生料入口和用于将经过换热后的生料引出至烟室111的第二生料出口。其中，第二换热装置140可以是现有技术装置。
烟气管道150连通至第一换热装置130。烟气管道150安装第一风机151，用于将经过换热后的烟气排出。正常情况下第一风机151以一定转速工作。
空气管道160连通至第二换热装置140。空气管道160安装第二风机161，用于将经过二次换热后的空气排出。正常情况下第二风机161以一定转速工作。
控制装置170分别连接至压力传感器114、气体分析仪115、第一风机151和第二风机161。当气体分析仪115监测的二氧化碳浓度大于阈值(即空气中二氧化碳含量为0.03％)时，控制装置170控制第一风机151的转速逐步提高，直至停留在使二氧化碳浓度降至阈值时的转速，期间压力传感器114监测的压力值处于预设范围值内，例如负10Pa-负35Pa之间。上述过程中，若控制第一风机151的转速逐步提高的过程中，压力传感器114监测的压力值大于预设范围值上限(即负35Pa)，控制装置170控制第二风机161的转速逐步降低，此时第一风机151的转速不变(即保持开始调整第二风机161转速时的转速)，直至第一风机151、第二风机161停留在使二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速。若控制第二风机161的转速逐步降低的过程中，压力传感器114监测的压力值小于预设范围值下限时二氧化碳浓度仍未降至阈值，控制装置170控制第一风机151的转速继续逐步提高，此时第二风机161的转速不变(即保持开始调整第一风机151转速时的转速)。重复上述过程，直至第一风机151、第二风机161停留在使二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速。
在上述过程中，控制装置170联合压力传感器114、气体分析仪115、第一风机151 和第二风机161所做的调整，目的在于实现回转窑110内的压力平衡点位于窑出口端(靠近窑头罩112)，这样回转窑110内生料受热分解产生的二氧化碳气体只经过回转窑110、烟室111和第一换热装置130而排出，与熟料换热的空气通过窑头罩112后只经过热风管道122和第二换热装置140而排出，两者不混合，保证了烟气中二氧化碳高浓度。
根据本公开的系统100，通过电磁感应装置113对回转窑110内的生料加热煅烧，生料分解释放二氧化碳气体，相较于传统的通过燃料燃烧方式，不带入空气，产生的二氧化碳烟气中二氧化碳浓度高；同时，通过控制装置170调控第一风机151和第二风机161的转速，控制二氧化碳浓度降至阈值和压力值降至预设范围值内，以使二氧化碳烟气和换热后的空气各自走各自的路径，不混合，进一步确保二氧化碳的高浓度；另外，整个系统100利用空气对熟料降温，又利用二氧化碳烟气、换热后的空气对生料预热，能量重复利用，能耗低。
参考图1，为了提供一种换热效果好的第一换热装置130，第一换热装置130可以包括从上往下布置的多个旋风筒180。旋风筒180的数量可以不做限制，例如可以是5个、6个或其他数量。其中，位于最下方的旋风筒180的底部物料出口连通至烟室111。位于最下方的旋风筒180的气体入口连通至烟室111。位于最上方的旋风筒180的顶部气体出口连通至烟气管道150。位于下方的旋风筒180的气体出口通过连接管道181连通至位于上方的旋风筒180。位于上方的旋风筒180的底部物料出口连通至下方的连接管道181。其中，生料投入至位于最上方的连接管道181。
继续参考图1，同样为了提供一种换热效果好的第二换热装置140，第二换热装置140也可以包括从上往下布置的多个旋风筒180。旋风筒180的数量可以不做限制，例如可以是5个、6个或其他数量。位于最下方的旋风筒180的底部物料出口连通至烟室111。位于最下方的旋风筒180的气体入口连通至热风管道122。位于最上方的旋风筒180的顶部气体出口连通至空气管道160。其中，位于下方的旋风筒180的气体出口通过连接管道181连通至位于上方的旋风筒180。位于上方的旋风筒180的底部物料出口连通至下方的连接管道181。其中，生料投入至位于最上方的连接管道181。
为了保证第一换热装置130、第二换热装置140基本相同的料气比，投入第一换热装置130和第二换热装置140的生料的比例为1∶(2-5)。例如第一换热装置130喂入约1/4生料，第二换热装置140喂入约3/4生料。
在优选实施方式中，烟气管道150排出的烟气还可以经由收尘器191进行除尘处 理。除尘处理后的烟气可连通至二氧化碳捕获系统192，以供二氧化碳捕获系统192使用。
进一步地，烟气管道150和空气管道160还可以连接至余热锅炉190，以进行余热利用。
下面将参考图1，以第一换热装置130、第二换热装置140均设置6个旋风筒180为例描述系统100的工作过程：
生料从第一换热装置130的旋风筒C2A与C1-A1、C1-A2之间的连接管道181，和C2B与C1-B1、C1-B2之间的连接管道181喂入，C2A与C1-A1、C1-A2之间的连接管道181喂入约1/4生料，C2B与C1-B1、C1-B2之间的连接管道181喂入3/4生料。生料在连接管道181内分散、换热，随气流进入C1-A1、C1-A2、C1-B1、C1-B2旋风筒，料气在旋风筒180中进行料气分离，气体从旋风筒180顶部排出，C1-A1、C1-A2旋风筒排出的是高浓度二氧化碳烟气，C1-B1、C1-B2旋风筒排出的是热空气。生料收集到旋风筒180锥部并且排出。
C1-A1、C1-A2旋风筒锥部排出的生料喂入C2A与C3A之间的连接管道181；C1-B1、C1-B2旋风筒锥部排出的生料喂入C2B与C3B之间的连接管道181。生料在连接管道181内分散、换热，随气流进入C2A、C2B旋风筒，料气在旋风筒180中进行料气分离，气体从旋风筒180顶部排出，C2A旋风筒排出的是高浓度二氧化碳烟气，C2B旋风筒排出的是热空气。生料收集到C2A、C2B旋风筒锥部并且排出。依次类推物料经过C3A、C3B，C4A、C4B，C5A、C5B，C6A、C6B旋风筒，加热后生料最终从C6A、C6B旋风筒锥部卸出喂入烟室111。
加热后生料喂入烟室111，然后进入回转窑110，高频交流电通过线圈产生交变磁场，使回转窑110产生涡流自发热。在窑内生料经过加热实现碳酸盐分解,物料在行进过程中的分解产物CaO与生料中的SiO2、Fe2O3、Al2O3等相互扩散进行固相反应，形成熟料矿物。物料从窑内通过，完成了以上熟料煅烧过程。在此过程中碳酸盐分解产生的二氧化碳气体从窑内、窑尾烟室111输送到旋风筒C6A的进口。
煅烧后的熟料喂入篦冷机120前段，熟料在篦冷机120上从进口到出口不断运动，同时与篦冷机120底部鼓风机121进入的空气进行热交换，完成熟料的冷却，和热量的回收，700-850度的高温热空气通过窑头罩112、热风管道122进入旋风筒C6B的进口。通过控制高温第一风机151和第二风机161的转速，实现窑内的压力平衡点位于窑出口 端(靠近窑头罩112)，实现窑内分解的CO2只走回转窑110内进入窑尾烟室111，高温热空气通过窑头罩112只进入热风管道122，实现了两种气体各自走各自的路径，不混合。
篦冷机120尾部多余的预热从尾部排除，可进入余热锅炉190或用于烘干物料等。
从旋风筒C1-A1、C1-A2出口经过换热的高浓度二氧化碳烟气进入行余热锅炉190，进行余热利用，然后进入高温第一风机151、收尘器191，喂入二氧化碳捕获系统192进一步进行二氧化碳提纯。从旋风筒C1-B1、C1-B2出口经过换热的热空气进行余热锅炉190，进行余热利用，然后进入高温第二风机161，喂入原料烘干及废气处理系统，最后除尘后从烟囱排出。
第二方面，本公开还提供一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法，基于上述技术方案的系统100。方法具体包括以下步骤：
生料在设置电磁感应装置113的回转窑110内受热分解产生二氧化碳气体，同时煅烧成熟料。
包含所分解产生的二氧化碳气体的烟气经由烟室111进入第一换热装置130。熟料经由窑头罩112进入风冷却装置与空气换热进行降温，换热后的空气进入第二换热装置140。
生料在进入回转窑110之前，分别投入第一换热装置130和第二换热装置140中与烟气和空气换热，换热后通过烟室111进入回转窑110煅烧，换热后的烟气和空气分别通过烟气管道150和空气管道160排出；其中，通过烟气管道150排出的烟气为高浓度二氧化碳烟气，烟气中二氧化碳浓度大于80％。
其中，当气体分析仪115监测的二氧化碳浓度大于阈值时，第一风机151逐步提高转速，直至停留在二氧化碳浓度降至阈值时的转速，且期间压力传感器114监测的压力值一直处于预设范围值内；上述过程中，若第一风机151在逐步提高转速的过程中，压力传感器114监测的压力值大于预设范围值上限但二氧化碳浓度未降至阈值，则第二风机161开始逐步降低转速，而第一风机151保持转速不变，直至第一风机151、第二风机161分别停留在二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速；上述过程中，若第二风机161在逐步降低转速的过程中，压力值小于预设范围值下限时二氧化碳浓度仍未降至阈值，第一风机151又继续逐步提高转速，而第二风机161保持转速不变；重复上述步骤，直至第一风机151、第二风机161停留在二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速。
结合这里披露的本公开的说明和实践，本公开的其他实施例对于本领域技术人员都是易于想到和理解的。说明和实施例仅被认为是示例性的，本公开的真正范围和主旨均由权利要求所限定。

Claims (9)

  1. 一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的系统，其特征在于，所述系统包括：
    回转窑，所述回转窑的尾部和头部分别设置烟室和窑头罩，所述回转窑沿长度方向环绕电磁感应装置；所述窑头罩内设置压力传感器和气体分析仪；
    风冷却装置，所述风冷却装置连通至所述窑头罩，用于利用空气冷却所述回转窑经由所述电磁感应装置加热煅烧生料所产生的熟料，所述窑头罩设置用于导出经过换热后的空气的热风管道；
    连通至所述烟室的第一换热装置，用于生料和所述回转窑煅烧生料所产生的烟气进行换热，所述第一换热装置包括用于引入生料的第一生料入口和用于将经过换热后的生料引出至所述烟室的第一生料出口；
    分别连通至所述烟室和所述热风管道的第二换热装置，用于生料和所述经过换热后的空气进行换热，所述第二换热装置包括用于引入生料的第二生料入口和用于将经过换热后的生料引出至所述烟室的第二生料出口；
    连通至所述第一换热装置的烟气管道，所述烟气管道安装第一风机，用于将经过换热后的烟气排出；
    连通至所述第二换热装置的空气管道，所述空气管道安装第二风机，用于将经过二次换热后的空气排出；
    其中，当气体分析仪监测的二氧化碳浓度大于阈值时，第一风机逐步提高转速，直至二氧化碳浓度降至阈值；若第一风机在逐步提高转速的过程中，压力传感器监测的压力值大于预设范围值上限，则第二风机开始逐步降低转速，直至二氧化碳浓度降至阈值和压力值降至预设范围值内；若第二风机在逐步降低转速的过程中，压力值小于预设范围值下限时二氧化碳浓度仍未降至阈值，第一风机又继续逐步提高转速；重复上述过程，直至二氧化碳浓度降至阈值和压力值降至预设范围值内。
  2. 根据权利要求1所述的系统，其特征在于，还包括：
    控制装置，所述控制装置分别连接至所述压力传感器、所述气体分析仪、所述第一风机和所述第二风机，所述控制装置用于：当所述气体分析仪监测的二氧化碳浓度大于 阈值时，控制所述第一风机的转速逐步提高，直至停留在能使二氧化碳浓度降至阈值时的转速，期间所述压力传感器监测的压力值处于预设范围值内；若控制所述第一风机的转速逐步提高的过程中，所述压力传感器监测的压力值大于预设范围值上限，控制所述第二风机的转速逐步降低，控制所述第一风机的转速不变，直至所述第一风机、所述第二风机停留在能使二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速；若控制所述第二风机的转速逐步降低的过程中，所述压力传感器监测的压力值小于预设范围值下限时二氧化碳浓度仍未降至阈值，控制所述第一风机的转速继续逐步提高，控制所述第二风机的转速不变；重复上述过程，直至所述第一风机、所述第二风机停留在能使二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速。
  3. 根据权利要求1或2所述的系统，其特征在于，所述第一换热装置包括从上往下布置的多个旋风筒，位于最下方的旋风筒的底部物料出口连通至所述烟室，位于最下方的旋风筒的气体入口连通至所述烟室，位于最上方的旋风筒的顶部气体出口连通至所述烟气管道；其中，位于下方的旋风筒的气体出口通过连接管道连通至位于上方的旋风筒，位于上方的旋风筒的底部物料出口连通至下方的所述连接管道；
    其中，生料投入至位于最上方的所述连接管道。
  4. 根据权利要求3所述的系统，其特征在于，所述第二换热装置也包括从上往下布置的多个旋风筒，位于最下方的旋风筒的底部物料出口连通至所述烟室，位于最下方的旋风筒的气体入口连通至所述热风管道，位于最上方的旋风筒的顶部气体出口连通至所述空气管道；其中，位于下方的旋风筒的气体出口通过连接管道连通至位于上方的旋风筒，位于上方的旋风筒的底部物料出口连通至下方的所述连接管道；
    其中，生料投入至位于最上方的所述连接管道。
  5. 根据权利要求4所述的系统，其特征在于，所述风冷却装置包括篦冷机，所述篦冷机的底部设置用于引入空气的鼓风机。
  6. 根据权利要求5所述的系统，其特征在于，投入所述第一换热装置和所述第二换热装置的生料的比例为1∶(2-5)。
  7. 根据权利要求1所述的系统，其特征在于，所述烟气管道排出的烟气还经由收尘器处理，处理后的烟气可连通至二氧化碳捕获系统。
  8. 根据权利要求1所述的系统，其特征在于，所述烟气管道和/或所述空气管道还 连接至余热锅炉。
  9. 一种基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法，基于如权利要求1至8中任一项所述的系统，其特征在于，所述方法包括：
    生料在设置电磁感应装置的回转窑内受热分解产生二氧化碳气体，同时煅烧成熟料；
    包含所分解产生的二氧化碳气体的烟气经由烟室进入第一换热装置，熟料经由窑头罩进入风冷却装置与空气换热进行降温，换热后的空气进入第二换热装置；
    生料在进入回转窑之前，分别投入第一换热装置和第二换热装置中与烟气和空气换热，换热后通过烟室进入回转窑煅烧，换热后的烟气和空气分别通过烟气管道和空气管道排出；其中，通过烟气管道排出的烟气为高浓度二氧化碳烟气，烟气中二氧化碳浓度大于80％；
    其中，当气体分析仪监测的二氧化碳浓度大于阈值时，第一风机逐步提高转速，直至停留在二氧化碳浓度降至阈值时的转速，且期间压力传感器监测的压力值一直处于预设范围值内；上述过程中，若第一风机在逐步提高转速的过程中，压力传感器监测的压力值大于预设范围值上限但二氧化碳浓度未降至阈值，则第二风机开始逐步降低转速，而第一风机保持转速不变，直至第一风机、第二风机分别停留在二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速；上述过程中，若第二风机在逐步降低转速的过程中，压力值小于预设范围值下限时二氧化碳浓度仍未降至阈值，第一风机又继续逐步提高转速，而第二风机保持转速不变；重复上述步骤，直至第一风机、第二风机停留在二氧化碳浓度降至阈值和压力值降至预设范围值内时的转速。
PCT/CN2024/082048 2023-09-15 2024-03-15 基于煅烧水泥熟料获得高浓度二氧化碳烟气的方法和系统 Pending WO2025055293A1 (zh)

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