WO2021026713A1 - 由在线型分解炉改造的可调节co2富集量水泥窑系统及其使用方法 - Google Patents

由在线型分解炉改造的可调节co2富集量水泥窑系统及其使用方法 Download PDF

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WO2021026713A1
WO2021026713A1 PCT/CN2019/100163 CN2019100163W WO2021026713A1 WO 2021026713 A1 WO2021026713 A1 WO 2021026713A1 CN 2019100163 W CN2019100163 W CN 2019100163W WO 2021026713 A1 WO2021026713 A1 WO 2021026713A1
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row
cyclone
preheaters
cyclone preheaters
calciner
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PCT/CN2019/100163
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English (en)
French (fr)
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何小龙
胡芝娟
彭学平
代中元
陈昌华
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天津水泥工业设计研究院有限公司
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Priority to PCT/CN2019/100163 priority Critical patent/WO2021026713A1/zh
Priority to CN201980054910.9A priority patent/CN112654590B/zh
Publication of WO2021026713A1 publication Critical patent/WO2021026713A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • 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
    • F27B17/00—Furnaces of a kind not covered by any preceding group
    • 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
    • F27B19/00—Combinations of furnaces of kinds not covered by a single preceding main group

Definitions

  • the invention belongs to the technical field of carbon emission reduction in the cement industry, and particularly relates to a cement kiln system and method with an adjustable CO 2 enrichment modified from an online calciner.
  • the current cement production process generally adopts the new dry production process, which is mainly composed of a cooler, a burner, a rotary kiln, a multi-stage cyclone preheater and connecting air ducts.
  • the raw meal is preheated in a cyclone preheater to increase the temperature, decomposed in the decomposition furnace, part of the fuel is burned in the decomposition furnace to provide the heat required for the decomposition of the raw meal, and the decomposed raw meal is calcined by another part of the fuel in the rotary kiln.
  • the cement clinker is cooled to a suitable temperature by a cooler.
  • the gas passing into the cement kiln system is air, and the CO 2 concentration at the outlet of the preheater is about 30%.
  • the technical solutions for carbon emission reduction in the cement industry are pre-combustion capture and post-combustion capture.
  • the pre-combustion capture refers to the pre-treatment of the fuel before combustion to separate the carbon in the fuel. Due to the characteristics of the cement clinker production process, a significant disadvantage of CO 2 capture before combustion is that only the CO 2 produced by fuel combustion can be separated, while about 60% of the CO 2 produced by the calcination of raw meal is emitted with the flue gas. The CO 2 has not received any treatment.
  • the post-combustion capture technology in the cement industry mainly refers to the capture or separation of CO 2 from the flue gas after combustion.
  • the main technologies include absorption, adsorption, membrane absorption, and mineral carbonization. Due to the low pressure, large volume flow, low CO 2 concentration, and a large amount of dust and N 2 in the flue gas of the cement industrial kiln, the above methods all have low carbon capture efficiency, small capture flow, complex systems, and large equipment investment Or the problem of high operating costs.
  • the present invention provides a cement kiln system with an adjustable CO 2 enrichment modified from an online calciner.
  • the cement kiln system includes: a first row of cyclone preheaters, a second row of cyclone preheaters, and a third row of cyclone preheaters.
  • the air inlets of the first row of cyclone preheaters and the second row of cyclone preheaters are connected to the first calciner; the outlet of the first row of cyclone preheaters or the outlet of the second row of cyclone preheaters are connected to the first Second decomposition furnace; the air inlet of the third row of cyclone preheaters is connected to the second decomposition furnace, and the discharge port of the penultimate first-stage cyclone of the third row of cyclone preheaters is connected to the smoke chamber;
  • the first decomposition furnace is connected with the smoke chamber, the smoke chamber is connected with the rotary kiln; the rotary kiln is connected with the cooler.
  • the hot raw material preheated by the first row of cyclone preheaters or the second row of cyclone preheaters or the first row of cyclone preheaters and the second row of cyclone preheaters can be distributed to the second decomposition furnace.
  • the discharge pipe of the penultimate cyclone separator of the second row of cyclone preheaters is provided with a first distribution valve, one end of the first distribution valve is connected to the first decomposition furnace, The other end of the split valve is connected to the second calciner.
  • the penultimate cyclone separator of the first row of cyclone preheaters is connected to the first calcining furnace through a pipe, and the pipe does not contain a branch or contains a branch;
  • the first row of cyclone preheaters feeds the first decomposition furnace at a single point
  • the pipeline When the pipeline includes branches, the first row of cyclone preheaters feeds the first decomposition furnace at multiple points; the pipeline includes a main conveying road and a conveying branch.
  • the number of conveying branches is more than two, and each conveying branch
  • the roads are connected in parallel, and the connection between the main conveying road and the conveying branch is provided with a second distributing valve; the second distributing valve is used to adjust the amount of material entering the conveying branch from the conveying main road.
  • the number of stages of the first row of cyclone preheaters and the number of stages of the second row of cyclone preheaters are selected from 3 to 7 stages;
  • the number of stages of the third row of cyclone preheaters is selected from 1 to 5 stages.
  • the cooling machine is selected from one of grate coolers, single-tube coolers, and multi-tube coolers;
  • the cement kiln system also includes a tertiary air pipe; one end of the tertiary air pipe is connected to the cooler, and the other end of the tertiary air pipe is connected to the first calciner.
  • the cement kiln system further includes a cooler, and the air outlet of the third row of cyclone preheaters is connected to a cooler; the cooler is used to cool the smoke discharged from the air outlet of the third row of cyclone preheaters gas.
  • the first row of cyclone preheaters and the second row of cyclone preheaters are both provided with feed ports, and the feed ports are provided in the first row of cyclone preheaters and the second row of cyclone preheaters.
  • the feed ports are provided in the first row of cyclone preheaters and the second row of cyclone preheaters.
  • the third row of cyclone preheater is equipped with or without feed inlet
  • the air outlet of the third row of cyclone preheaters is connected to the cooler, and at this time, the third row of cyclone preheaters are not provided with an inlet;
  • the third row of cyclone preheaters are provided with a feed inlet;
  • the feed inlet of the third row of cyclone preheaters is arranged at the top of the third row of cyclone preheaters and the inlet of the first stage cyclone separator Air duct
  • the feed inlet of the third row of cyclone preheaters is set on the top of the third row of cyclone preheaters, and the inlet duct of the first stage cyclone separator Or set at the inlet duct of the top second cyclone separator of the third row of cyclone preheaters.
  • a communication pipe is provided between the third row of cyclone preheaters and the first row of cyclone preheaters, and / Or a connecting pipe is arranged between the third row of cyclone preheaters and the second row of cyclone preheaters;
  • the communicating pipe is used to transport the raw meal preheated by the third row of cyclone preheaters to the first row of cyclones The preheater or the second row of cyclone preheaters, or simultaneous delivery to the first row of cyclone preheaters and the second row of cyclone preheaters;
  • One end of the communicating pipe is arranged at the discharge port of the penultimate cyclone separator of the third row of cyclone preheaters;
  • the other end of the communicating pipe is arranged on the inlet duct of the first cyclone separator on the top of the first row of cyclone preheaters or the second row of cyclone preheaters, or is arranged on the first row of cyclone preheaters or the first row of cyclone preheaters.
  • the cement kiln system further includes a heat exchanger, the tertiary air pipe is divided into two paths, one end of the tertiary air pipe is connected to the cooler, and the other end of the tertiary air pipe is connected to the first decomposition Furnace; the other end of the tertiary air pipe is connected to the heat exchanger, and the heat exchanger is connected to the second calciner through a pipe.
  • dividing the tertiary air pipe into two paths can be achieved by arranging two pipes, or by arranging a main road and a branch circuit on the tertiary air pipe.
  • one end of the two pipes is connected to the cooling machine; the other end of the first pipe is connected to the first decomposition furnace, the other end of the second pipe is connected to the heat exchanger, and the heat exchanger passes through the pipe Connect the second calciner;
  • one end of the main circuit is connected to the cooler, the other end of the main circuit is connected to the first calciner; one end of the branch circuit is connected to the main circuit, and the other end of the branch circuit is connected to the heat exchanger ,
  • the heat exchanger is connected to the second calciner through a pipeline.
  • the present invention also provides a method for preparing cement clinker using the above-mentioned cement kiln system with adjustable CO 2 enrichment modified from an online calciner, and the method includes:
  • the raw meal is added to the first row of cyclone preheaters and the second row of cyclone preheaters respectively, and the raw meal exchanges heat with the flue gas in the cyclone preheater;
  • the raw meal preheated by the first row of cyclone preheaters and the second row of cyclone preheaters enter the first decomposition furnace through one or more points; the first row of cyclone preheaters or the second row of cyclone preheaters or the first Part of the hot raw meal preheated by the cyclone preheater in the second row and the second row enters the second calciner through one or more points;
  • the decomposed hot raw meal leaves the first calciner and the second calciner, and then enters the rotary kiln after being separated from the flue gas, and is calcined in the rotary kiln to form cement clinker.
  • the clinker enters the cooler from the outlet of the rotary kiln;
  • the mixed gas of oxygen and circulating flue gas or oxygen is transported to the second calcining furnace.
  • the second calcining furnace is oxy-fuel or all-oxygen combustion.
  • the high CO 2 concentration flue gas produced in the second calcining furnace passes through the third column
  • the cyclone preheater is discharged; the CO 2 enrichment amount can be adjusted by adjusting the amount of hot raw material into the second decomposition furnace.
  • the raw meal can be added or not added to the third row of cyclone preheaters.
  • the raw meal preheated by the second row of cyclone preheaters is divided into two paths through the first split valve, one path enters the first calciner, and the other path enters the second calciner.
  • the raw meal is fed into the first row of cyclone preheaters, the second row of cyclone preheaters, the first row of cyclone preheaters and the second row of cyclone preheaters.
  • Enter the first calciner adjust the amount of hot raw material delivered to the second calciner through the first distributing valve.
  • the second calciner is oxy-fuel or oxy-fuel combustion.
  • the system is CO 2 self-enriching In the decomposition kiln, the CO 2 enrichment amount can be adjusted by adjusting the amount of hot raw material entering the second decomposition furnace by the first distributing valve;
  • the raw meal preheated by the first row of cyclone preheaters and the second row of cyclone preheaters enter the first calciner and adjust
  • the first distribution valve makes the raw meal preheated by the second row of cyclone preheaters to be transported to the first calciner, and the second calciner, the third row of cyclone preheaters, and coolers are out of service.
  • the system is normal Online precalcining kiln.
  • the raw meal preheated by the third row of cyclone preheaters enters the first row of cyclone preheaters or the second row of cyclone preheaters through the connecting pipe. Heater, or enter the first row of cyclone preheaters and the second row of cyclone preheaters simultaneously.
  • the air cools the high-temperature clinker through the cooler and the air after the heat exchange includes the following three paths: the first high-temperature air directly enters the rotary kiln as the secondary air for fuel Combustion; the second high-temperature air directly enters the first calciner as the tertiary air for fuel combustion; the third high-temperature air enters the waste heat boiler for power generation or other waste heat utilization or processing systems, power generation is completed or other waste heat utilization or processing systems
  • the flue gas is treated by the residual air and discharged into the atmosphere through the chimney.
  • the second path of high temperature air is divided into two paths as tertiary air.
  • One path of tertiary air enters the first calciner through the tertiary duct; the other path of tertiary air enters the heat exchanger through the tertiary duct, and oxygen
  • the mixed gas or oxygen with the circulating flue gas enters the heat exchanger, and the mixed gas or oxygen of the oxygen and the circulating flue gas after the heat exchange enters the second calciner through the pipe, and the second calciner is oxy-fuel combustion or full-oxygen combustion;
  • the tertiary air after heat exchange enters the waste heat utilization or treatment system;
  • the waste heat utilization or processing system includes waste heat power generation and drying materials.
  • the present invention has the following advantages and effects:
  • the system can be switched to a CO 2 self-enriching precalciner kiln or a conventional online precalciner kiln.
  • a CO 2 self-enriching precalciner kiln or a conventional online precalciner kiln Although the implementation of carbon emission reduction in the cement industry is a general trend, China's current market demand for food-grade or industrial-grade CO 2 products is limited. Taking a 5500t/d cement clinker production line as an example, if all CO 2 in the kiln tail gas is captured and purified into food-grade or industrial-grade CO 2 products, it will be sufficient to meet the vast majority of China’s CO 2 needs. At present, there are more than 1,000 cement clinker production lines of different scales in China.
  • the components of the system of the present invention can be adjusted according to the demand for CO 2 products, and then the CO 2 enrichment of the cement kiln system can be flexibly adjusted to achieve carbon emission reduction in the cement industry.
  • the demand for CO 2 products is not high, the cement kiln may not carry out CO 2 self-enrichment, which will not affect the normal production of cement clinker;
  • the cement kiln system of the present invention can carry out CO 2 enrichment without redesigning key firing equipment such as rotary kilns and coolers, greatly simplifying the process flow, reducing the cost of transformation, and being suitable for most existing pre-treatment renovation of the calcining kiln system or design of a new precalcining kiln system;
  • the CO 2 concentration in the flue gas at the outlet of the first row of cyclone preheaters and the second row of cyclone preheaters is about 30%, and the third row of cyclone preheaters
  • Figure 1 is a diagram of a cement kiln with adjustable CO 2 enrichment modified from an online calciner in Example 1 of the present invention
  • Figure 2 is a diagram of a cement kiln with adjustable CO 2 enrichment modified from an online calciner in Example 2 of the present invention
  • Figure 3 is a partial schematic diagram of the tertiary air duct in Example 3.
  • connection should be understood in a broad sense, for example, it may be a fixed connection, a detachable connection, or an integral Ground connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, and it can be a connection between two components.
  • connection should be understood in specific situations.
  • the cement kiln system with adjustable CO 2 enrichment includes column A cyclone preheater, column B cyclone preheater, column C cyclone preheater, decomposition furnace A (5), decomposition furnace B ( 8) Smoke chamber (15), rotary kiln (14), cooler (12); the air inlets of column A cyclone preheater and column B cyclone preheater are all connected to calciner A (5), column A cyclone preheater
  • the discharge port of the penultimate cyclone separator of column B cyclone preheater is connected to smoke chamber (15); the air inlet of column C cyclone preheater is connected to decomposition furnace B (8), column C cyclone preheater
  • the discharge port of the heater is connected to the smoke chamber (15); the decomposition furnace A (5) is connected to the smoke chamber (15), and the smoke chamber (15) is connected to the rotary kiln (14); the rotary kiln (14) and the cooler (12)
  • Decomposing furnace A (5) and decomposition furnace B (8) are equipped with a decomposing furnace burner (4); a rotary kiln (14) is provided with a rotary kiln burner (11); a cooling machine (12) is provided There is a tertiary air duct (10); a fan (13) is arranged under the cooler (12).
  • the discharge pipe of the penultimate cyclone separator of column B cyclone preheater is provided with a first distributing valve (7), one end of the first distributing valve (7) is connected to the decomposition furnace A (5), The other end of the split valve (7) is connected to the decomposition furnace B (8).
  • the penultimate cyclone separator of column A cyclone preheater is connected to decomposition furnace A (5) through a pipeline, the pipe contains a branch, and the cyclone preheater of column A feeds decomposition furnace A (5) at multiple points;
  • the pipeline includes a main conveying road and a conveying branch.
  • the number of conveying branches is more than two.
  • Each conveying branch is connected in parallel, and a second distribution valve (6) is provided at the junction of the conveying main road and the conveying branch;
  • One end of the second split valve (6) is connected to the main conveying road, and the other ports of the second split valve (6) are connected to the conveying branch; The amount of material.
  • the cooler (12) is selected from one of grate coolers, single-tube coolers, and multi-tube coolers;
  • the column A cyclone preheater, column B cyclone preheater, and column C cyclone preheater are all equipped with feed inlets.
  • the feed inlet (2) and the feed inlet (3) of the cyclone preheater of column C are arranged at the top of the cyclone preheater of column A, the cyclone preheater of column B, and the first cyclone separator of column C. At the inlet duct.
  • the feed inlet can also be arranged at the inlet duct of the uppermost second-stage cyclone of the cyclone preheater of column A, column B and cyclone preheater of column C.
  • the column C cyclone preheater can be provided with or without a feed port. Specifically, when the number of stages of the column C cyclone preheater is 2, the feed inlet of the column C cyclone preheater is set at the inlet duct of the first stage cyclone separator on the top of the column C cyclone preheater .
  • the feed inlet of the column C cyclone preheater is set at the inlet duct of the first stage cyclone separator on the top of the column C cyclone preheater, or It is set at the inlet duct of the second stage cyclone separator on the top of the column C cyclone preheater.
  • a communication pipe is provided between the column C cyclone preheater and the column B cyclone preheater, and the communication pipe is used to transport the raw meal preheated by the column C cyclone preheater to the column B cyclone preheater.
  • a connecting pipe may be provided between the column C cyclone preheater and the column A cyclone preheater, and/or a connecting pipe may be provided between the column C cyclone preheater and the column B cyclone preheater;
  • the connecting pipeline is used to transport the raw meal preheated by the cyclone preheater of column C to the cyclone preheater of column A or the cyclone preheater of column B, or to the cyclone preheater of column A and cyclone preheater of column B at the same time .
  • the system can be switched to CO 2 self-enrichment precalciner kiln or conventional online precalciner kiln. Specifically, the system can be switched to any of the following three situations through the adjustment of components.
  • the first case feed the raw meal through the feed port (1) of the cyclone preheater column A, the feed port (2) of the cyclone preheater column B, and the feed port (3) of the cyclone preheater column C Feed into the system, and distribute the hot raw material in the column B cyclone preheater to the decomposition furnace A (5) and decomposition furnace B (8) through the first distributing valve (7), and the oxygen enters the decomposition furnace B
  • the tuyere (9) enters the decomposition furnace B (8), the decomposition furnace B (8) is full-oxygen combustion, and the system is a CO 2 self-enrichment type precalciner.
  • the raw meal is fed into the cyclone preheater of column A, column B and column C by the feeding device through the elevator, and the preheating and gas-solid separation are realized in the cyclone preheater.
  • the raw meal in column A enters the decomposition furnace A(5) from the penultimate cyclone separator in column A (5).
  • the raw meal in column B is divided into two paths in the first feed valve (7), one of which enters the decomposition furnace A (5) and the other one enters the decomposition furnace B (8).
  • the raw meal fed into the cyclone preheater of column C is used to cool the high-temperature flue gas discharged from the decomposition furnace B (8).
  • the raw meal preheated by the cyclone preheater of column C enters the cyclone preheater of column B through the connecting pipe.
  • One end of the communicating pipe is set at the discharge port of the penultimate cyclone separator of column C cyclone preheater, and the other end of the communicating pipe is set on the inlet duct of the first cyclone separator on the top of column B cyclone preheater .
  • the raw meal that has been preheated in column C can be fed into column B cyclone preheater or column A cyclone preheater through connecting pipes, or into column A cyclone preheater and column B cyclone preheater at the same time, and connected pipe into A
  • the feed point of the row cyclone preheater or row B cyclone preheater can be set on the inlet air pipe of the first cyclone separator on the top of row A cyclone preheater or row B cyclone preheater, or set on the inlet duct of the first cyclone separator of row A Column cyclone preheater or column B cyclone preheater on the uppermost second-stage cyclone inlet pipe, or set on the uppermost third-stage cyclone separator of column A or B cyclone preheater
  • the fuel combustion in the calciner releases a large amount of heat for the decomposition of the raw meal.
  • the hot raw meal after decomposition leaves the calciner A (5) and the calciner B (8), and then enters the rotary kiln (14) after being separated from the flue gas.
  • the clinker Internal calcined mature material, the clinker enters the cooler (12) from the outlet of the rotary kiln (14), and then is cooled to 65°C + ambient temperature by the cooler (12).
  • the air is cooled by the cooler (12) for the high-temperature clinker, and the air after the heat exchange is mainly divided into the following three paths:
  • the first high-temperature air (900 ⁇ 1200°C) is directly supplied into the rotary kiln (14) as the secondary air Fuel combustion;
  • the second high-temperature air (800 ⁇ 1000°C) enters the calciner A(5) as the tertiary air through the tertiary air pipe for fuel combustion;
  • the third high temperature air 250 ⁇ 450°C
  • the flue gas from boiler power generation or other waste heat utilization or treatment system, power generation or other waste heat utilization or treatment system is discharged into the atmosphere through the chimney after the waste air treatment.
  • the pure oxygen produced by the air separation device enters the decomposition furnace B (8) for fuel combustion in the decomposition furnace B (8), and the decomposition furnace B (8) is fully oxy-fueled.
  • the flue gas formed by fuel combustion and raw meal decomposition in the calciner B (8) leaves the calciner B (8) and enters the cyclone preheater of column C.
  • the raw meal of column C is then preheated and gas-solid separated, and finally from the cyclone of column C The outlet of the preheater leaves.
  • the concentration of CO 2 in the flue gas leaving from the flue gas outlet (18) of the cyclone preheater of column C is> 70%, and the flue gas temperature is based on the number of cyclone separator stages set in the cyclone preheater of column C and the cyclone preheater of column C
  • the feed amount of the raw meal is controlled, and a series of operations such as drying and dust removal and CO 2 capture and purification of this part of the flue gas can obtain CO 2 products with a concentration of more than 99% for resource utilization.
  • the kiln gas formed by fuel combustion and partial raw meal decomposition in the rotary kiln (14) enters the decomposition furnace A (5), and the flue gas formed by the fuel combustion and raw meal decomposition in the decomposition furnace A (5) and the flue gas from the rotary kiln (14)
  • the kiln gas leaves the calciner A (5) together and enters the cyclone preheaters of column A and column B. Then the raw materials of column A and B are preheated and separated from gas and solid, and finally from the cyclone preheater of column A.
  • the flue gas outlet (16) and the flue gas outlet (17) of the column B cyclone preheater leave.
  • the CO 2 concentration in the flue gas leaving from the outlets of the cyclone preheaters of columns A and B is about 30%, and the temperature of the flue gas is 300-400°C. Then the flue gas is passed through the kiln tail waste heat boiler to generate electricity and enters the raw meal mill for drying The raw meal is then discharged into the atmosphere after being processed by the flue gas treatment system.
  • the CO 2 enrichment amount can be adjusted by adjusting the amount of hot raw material entering the decomposition furnace B (8) by the first split valve (7).
  • the second case the adjustment of the system components, the flow direction of materials and gases are the same as the first case, the difference is that part of the flue gas discharged from the outlet of the cyclone preheater of column C is used as the circulating flue gas, and the circulating flue gas is The oxygen mixed gas enters the decomposition furnace B (8) through the air inlet (9) of the decomposition furnace B, and the decomposition furnace B (8) is oxygen-enriched combustion, and the system is a CO 2 self-enrichment type precalciner.
  • the CO 2 concentration in the flue gas discharged from the outlet of the cyclone preheater column A and the outlet of the cyclone preheater column B is about 30%, and the CO 2 concentration in the flue gas discharged from the outlet of the cyclone preheater column C>70%.
  • the CO 2 enrichment amount can be adjusted by adjusting the feed amount of the first feed valve (7) into the decomposition furnace B (8).
  • the third case the raw meal is fed into the cyclone preheaters of row A and row B, and the cyclone preheater of row C no longer feeds raw meal.
  • the raw meal of row A and row B are all fed into the decomposition furnace A (5 ), decomposing furnace B(8) and column C cyclone preheaters are out of service, and the system is a conventional online precalcining kiln.
  • the CO 2 concentration in the flue gas discharged from the outlet of the cyclone preheater of column A and the outlet of the cyclone preheater of column B is about 30%, and the temperature of the flue gas is 300-400°C.
  • the connection relationship of the components of the system is the same as that of Example 1.
  • the difference is that the number of stages of the cyclone preheater of column C is 1, and the air outlet of the cyclone preheater of column C is connected to the cooler (19 ), the cooler (19) is used to cool the flue gas discharged from the column C cyclone preheater, and the cooled flue gas is discharged from the flue gas outlet (20) of the cooler.
  • a CO 2 product with a concentration greater than 99% for resource utilization can be obtained.
  • the hot raw material in the cyclone preheater of column B is sent to the decomposition furnace A (5) and the decomposition furnace B (8) through the first distribution valve (7), and the decomposition can be adjusted through the first distribution valve (7)
  • the amount of materials in the furnace B (8) adjusts the amount of CO 2 enrichment.
  • the system can be switched to CO 2 self-enrichment precalciner kiln or conventional online precalciner kiln. Specifically, the system can be switched to any of the following three situations through the adjustment of components.
  • the first case feed the raw meal into the system through the feed port (1) of the cyclone preheater column A and the feed port (2) of the cyclone preheater column B, and pass the first split valve (7 ) Distribute the hot raw materials in the cyclone preheater of column B to the decomposition furnace A (5) and decomposition furnace B (8).
  • the oxygen enters the decomposition furnace B (8) through the air inlet (9) of the decomposition furnace B, and the decomposition furnace B(8) is full-oxygen combustion, and the system is a CO 2 self-enriching precalciner.
  • the CO 2 concentration in the flue gas discharged from the outlet of the cyclone preheater column A and the outlet of the cyclone preheater column B is about 30%, and the CO 2 concentration in the flue gas discharged from the cyclone preheater outlet of column C>70%.
  • the raw material decomposed by the decomposition furnace B (8) enters the connected C cyclone separator through the pipe for gas-solid separation, the separated material is transported to the smoke chamber (15) through the pipe, and the separated gas enters the cooling through the pipe Cooling is performed in the device (19), and the CO 2 concentration in the flue gas after cooling is> 70%.
  • the second case the adjustment of the system components, the flow direction of materials and gases are the same as the first case, the difference is that part of the flue gas discharged from the outlet of the cooler (19) is used as the circulating flue gas, and the flue gas and oxygen are circulated
  • the mixed gas enters the decomposition furnace B (8) through the air inlet (9) of the decomposition furnace B, and the decomposition furnace B (8) is oxy-fuel combustion, and the system is a CO 2 self-enriching precalciner kiln.
  • the CO 2 concentration in the flue gas discharged from the outlet of the cyclone preheater column A and the outlet of the cyclone preheater column B is about 30%, and the CO 2 concentration in the flue gas discharged from the outlet of the cyclone preheater column C is >70%.
  • the CO 2 enrichment amount can be adjusted by adjusting the feed amount of the first feed valve (7) into the decomposition furnace B (8).
  • the third case the raw meal is fed into the cyclone preheaters of row A and row B, and the cyclone preheater of row C no longer feeds raw meal.
  • the raw meal of row A and row B are all fed into the decomposition furnace A (5 ), decomposing furnace B (8), column C cyclone preheater and cooler (19) are out of service, and the system is a conventional online precalcining kiln.
  • the concentration of CO 2 in the flue gas discharged from the outlet of the cyclone preheater of row A and the outlet of the cyclone preheater of row B is about 30%.
  • a tertiary air duct (10) is provided on the cooler (12).
  • the tertiary air duct (10) is divided into two ways. One end of the tertiary air duct (10) is connected to the cooler (12). The other end of the air pipe (10) is connected to the decomposition furnace A (5); the other end of the tertiary air pipe (10) is connected to the heat exchanger (21), and the heat exchanger (21) is connected to the decomposition furnace B (8 ).
  • the heat exchanger (21) is provided with a gas inlet (2101) and a gas outlet (2102).
  • the gas outlet (2102) is connected to a waste heat utilization or processing system, which includes waste heat power generation, drying materials, and the like.
  • the mixed gas or oxygen of oxygen and circulating flue gas is delivered to the heat exchanger (21) through the gas inlet (2101), the tertiary air is delivered to the heat exchanger (21) through the tertiary air pipe (10), and the oxygen and the circulating flue gas
  • the tertiary air after the heat exchange enters the waste heat utilization or treatment system through the gas outlet (2102), and the mixed gas or oxygen of the oxygen and the circulating flue gas after the heat exchange enters the decomposition furnace B (8) through the pipe.
  • the tertiary air preheats the oxygen in the heat exchanger (21).
  • the preheated oxygen enters the decomposition furnace B (8), and the decomposition furnace B (8) contains all Oxygen combustion.
  • the tertiary air preheats the mixed gas of oxygen and circulating flue gas in the heat exchanger (21), and the completed oxygen and circulating flue gas are preheated.
  • the gas mixture enters the decomposition furnace B (8), and the decomposition furnace B (8) is oxygen-enriched combustion.
  • the tertiary air duct (10) and heat exchanger (21) in Embodiment 3 can be applied to Embodiment 1 or Embodiment 2 or a known cement kiln system.

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Abstract

本发明涉及由在线型分解炉改造的可调节CO 2富集量水泥窑系统及其使用方法。通过本发明部件的调节功能，可以使系统切换为CO 2自富集型预分解窑或常规在线型预分解窑。本发明可根据CO 2的需求量调节系统的部件，进而灵活调节水泥窑系统CO 2富集量。而且，本发明的水泥窑系统无需对关键烧成设备进行重新设计，即可进行CO 2富集，降低改造成本。此外，当本发明系统作为CO 2自富集型预分解窑时，第三列旋风预热器出口烟气中CO 2浓度＞70%，可大大降低后续CO 2捕集提纯和运行成本，且高CO 2浓度的烟气量可灵活调整为常规预分解窑系统预热器出口烟气量的5~30%，大大降低了预分解窑系统的CO 2排放量。

Description

[根据细则37.2由ISA制定的发明名称]　由在线型分解炉改造的可调节CO2富集量水泥窑系统及其使用方法 技术领域
本发明属于水泥工业碳减排技术领域，尤其涉及由在线型分解炉改造的可调节CO 2富集量水泥窑系统及方法。
背景技术
作为一种主要的温室气体，CO 2的大量排放加剧了全球温室效应，世界各国均普遍面临着实现碳减排、缓解全球气候变化的艰巨任务。为更好发展全球经济和保护自然环境，世界各国都相继制定了碳减排战略目标。在中国，水泥行业已成为仅次于电力行业的第二大CO 2排放源。据统计，2018年中国水泥熟料产量接近19亿吨，在现有每生产1吨水泥熟料的CO 2排放量约为0.84吨的技术水平条件下，CO 2排放量在2018年已达到15.96亿吨。因此，减缓水泥工业高CO 2排放问题刻不容缓。对碳减排技术的研究，国内外已有不少报导，但这些研究主要面向电力、煤炭和钢铁等行业，水泥行业相关的碳减排技术报导相对较少。当前水泥生产工艺普遍采用的是新型干法生产工艺，它主要由冷却机、燃烧器、回转窑、多级旋风预热器和连接风管等组成。其中，生料在旋风预热器中预热升温，在分解炉内分解，部分燃料在分解炉燃烧提供生料分解所需的热量，分解后的生料在回转窑内由另一部分燃料煅烧成水泥熟料，随后水泥熟料经冷却机冷却至合适温度。当前通入水泥窑系统的气体为空气，预热器出口CO 2浓度为30％左右。目前水泥行业可采用的碳减排技术方案为燃烧前捕集和燃烧后捕集。其中燃烧前捕集是指对燃料在燃烧前进行预处理，分离出燃料中的碳。由于水泥熟料生产工艺特点，燃烧前CO 2捕集的一个显著缺点是仅能分离出燃料燃烧产生的CO 2，而生料煅烧产生的约60％的CO 2随烟气排放了，这部分的CO 2没有得到任何处理。此外，燃烧前捕集技术相比其他CO 2捕集技术熟料煅烧过程对氢燃烧的条件非常苛刻，需要对回转窑燃烧器进行特殊设计，因此该技术在水泥行业中可行性较低，可以被排除。水泥行业燃 烧后捕集技术主要是指对燃烧后的烟气进行捕集或者分离出CO 2，主要的技术包括吸收法、吸附法、膜吸收法和矿物碳化法等。由于水泥工业窑尾烟气的压力小、体积流量大、CO 2浓度低，且含有大量的粉尘和N 2，上述方法均存在碳捕集效率低、捕集流量小、系统复杂、设备投资大或者运行成本偏高的问题。
发明内容
针对上述问题，本发明提供由在线型分解炉改造的可调节CO 2富集量水泥窑系统，所述水泥窑系统包括：第一列旋风预热器、第二列旋风预热器、第三列旋风预热器、第一分解炉、第二分解炉、烟室、回转窑、冷却机；
第一列旋风预热器、第二列旋风预热器的进风口均连接第一分解炉；第一列旋风预热器的出料口或第二列旋风预热器的出料口连接第二分解炉；第三列旋风预热器的进风口连接第二分解炉，第三列旋风预热器的倒数第一级旋风分离器的出料口连接烟室；
第一分解炉与烟室相连接，烟室连接回转窑；回转窑与冷却机相连接。
根据本发明，可以将第一列旋风预热器或第二列旋风预热器或第一列旋风预热器和第二列旋风预热器预热完成的热生料部分分配至第二分解炉。
根据本发明的实施方案，第二列旋风预热器的倒数第二级旋风分离器的下料管处设置有第一分料阀，第一分料阀的一端连第一分解炉，第一分料阀的另一端连接第二分解炉。
根据本发明的实施方案，第一列旋风预热器的倒数第二级旋风分离器通过管道连接第一分解炉，所述管道不包含支路或包含支路；
所述管道不包含支路时，第一列旋风预热器对第一分解炉单点进料；
所述管道包含支路时，第一列旋风预热器对第一分解炉多点进料；所述管道包括输送干路和输送支路，输送支路的数量为2个以上，各个输送 支路之间并联，输送干路与输送支路的连接处设置有第二分料阀；第二分料阀用于调节由输送干路进入输送支路的物料量。
根据本发明的实施方案，第一列旋风预热器的级数、第二列旋风预热器的级数选自3～7级；
第三列旋风预热器的级数选自1～5级。
根据本发明的实施方案，冷却机选自篦式冷却机、单筒冷却机、多筒冷却机中的一种；
所述水泥窑系统还包括三次风管；所述三次风管的一端连接冷却机，所述三次风管的另一端连接第一分解炉。
根据本发明的实施方案，所述水泥窑系统还包括冷却器，第三列旋风预热器的出风口连接冷却器；所述冷却器用于冷却由第三列旋风预热器出风口排出的烟气。
根据本发明的实施方案，所述第一列旋风预热器、第二列旋风预热器上均设置有进料口，所述进料口设置在第一列旋风预热器、第二列旋风预热器的最上面第一级旋风分离器的进口风管处，或者设置在第一列旋风预热器、第二列旋风预热器最上面第二级旋风分离器的进口风管处；
第三列旋风预热器上设置或不设置进料口；
当第三列旋风预热器的级数为1级时，第三列旋风预热器的出风口连接冷却器，此时第三列旋风预热器上不设置进料口；
当第三列旋风预热器的级数为2级以上时，第三列旋风预热器上设置进料口；
具体地，当第三列旋风预热器的级数为2级时，第三列旋风预热器的进料口设置在第三列旋风预热器的最上面第一级旋风分离器的进口风管处；
当第三列旋风预热器的级数为3级以上时，第三列旋风预热器的进料口设置在第三列旋风预热器的最上面第一级旋风分离器的进口风管处，或 者设置在第三列旋风预热器的最上面第二级旋风分离器的进口风管处。
根据本发明的实施方案，当所述第三列旋风预热器级数为2级以上时，所述第三列旋风预热器与第一列旋风预热器之间设置有连通管道，和/或第三列旋风预热器与第二列旋风预热器之间设置有连通管道；所述连通管道用于将第三列旋风预热器预热完成的生料输送至第一列旋风预热器或第二列旋风预热器，或者同时输送至第一列旋风预热器和第二列旋风预热器中；
所述连通管道的一端设置在第三列旋风预热器倒数第二级旋风分离器的出料口处；
所述连通管道的另一端设置在第一列旋风预热器或第二列旋风预热器最上面第一级旋风分离器的进口风管上，或者设置在第一列旋风预热器或第二列旋风预热器最上面第二级旋风分离器的进口风管上，或者设置在第一列旋风预热器或第二列旋风预热器最上面第三级旋风分离器的进口风管上，或者设置在第一列旋风预热器或第二列旋风预热器最上面第四级旋风分离器的进口风管上，或者设置在第一列旋风预热器或第二列旋风预热器最上面第五级旋风分离器的进口风管上。
根据本发明的实施方案，所述水泥窑系统还包括热交换器，所述三次风管分为两路，三次风管的一端连接冷却机，其中一路为三次风管的另一端连接第一分解炉；另一路为三次风管的另一端连接热交换器，热交换器通过管道连接第二分解炉。
例如，三次风管分为两路可以通过设置两条管道实现，或者通过在三次风管上设置主路、支路实现。
具体地，当设置两条管道时，两条管道的一端均连接冷却机；第一条管道的另一端连接第一分解炉，第二条管道的另一端连接热交换器，热交换器通过管道连接第二分解炉；
当在三次风管上设置主路、支路时，主路的一端连接冷却机，主路的另一端连接第一分解炉；支路的一端连接主路，支路的另一端连接热交换 器，热交换器通过管道连接第二分解炉。
本发明还提供使用上述由在线型分解炉改造的可调节CO 2富集量水泥窑系统制备水泥熟料的方法，所述方法包括：
将生料分别加入第一列旋风预热器、第二列旋风预热器，生料在旋风预热器内与烟气进行换热；
第一列旋风预热器和第二列旋风预热器预热后的生料通过一点或多点进入第一分解炉；第一列旋风预热器或第二列旋风预热器或第一列和第二列旋风预热器预热后的部分热生料通过一点或多点进入第二分解炉；
分解完成的热生料离开第一分解炉、第二分解炉，随后与烟气分离后进入回转窑，在回转窑内煅烧形成水泥熟料，熟料由回转窑出口进入冷却机；
将氧气与循环烟气的混合气体或氧气输送到第二分解炉内，第二分解炉内为富氧燃烧或全氧燃烧，第二分解炉内产生的高CO 2浓度烟气经第三列旋风预热器排出；通过调节进第二分解炉的热生料量能够调节CO 2富集量。
根据本发明，生料可以加入或不加入第三列旋风预热器。
根据本发明的实施方案，第二列旋风预热器预热后的生料通过第一分料阀分为两路，一路进入第一分解炉，另一路进入第二分解炉。
根据本发明的实施方案，将生料分别喂入第一列旋风预热器、第二列旋风预热器，第一列旋风预热器和第二列旋风预热器预热后的生料进入第一分解炉，通过第一分料阀调节向第二分解炉内输送热生料量，第二分解炉内为富氧燃烧或全氧燃烧，此时系统为CO 2自富集型预分解窑，通过调节第一分料阀进第二分解炉的热生料量能够调节CO 2富集量；
将生料分别喂入第一列旋风预热器、第二列旋风预热器，第一列旋风预热器和第二列旋风预热器预热后的生料进入第一分解炉，调节第一分料阀使第二列旋风预热器预热后的生料全部输送到第一分解炉，第二分解炉、 第三列旋风预热器、冷却器停止使用，此时系统为常规在线型预分解窑。
根据本发明的实施方案，生料喂入第三列旋风预热器时，第三列旋风预热器预热后的生料通过连通管道进入第一列旋风预热器或第二列旋风预热器，或者同时进入第一列旋风预热器和第二列旋风预热器。
根据本发明的实施方案，按气体流向而言，空气经冷却机对高温熟料进行冷却，换热完成的空气包括以下三路：第一路高温空气作为二次风直接进入回转窑内供燃料燃烧；第二路高温空气作为三次风直接进入第一分解炉内供燃料燃烧；第三路温度较高的空气进入余热锅炉发电或其他余热利用或处理系统，发电完成或其他余热利用或处理系统的烟气通过余风处理后经烟囱排入大气。
根据本发明的实施方案，所述第二路高温空气作为三次风分为两路，其中一路三次风通过三次风管进入第一分解炉；另一路三次风通过三次风管进入热交换器，氧气和循环烟气的混合气体或氧气进入热交换器，热量交换完成的氧气和循环烟气的混合气体或氧气通过管道进入第二分解炉，第二分解炉内为富氧燃烧或全氧燃烧；热量交换完成的三次风进入余热利用或处理系统；
所述余热利用或处理系统包括余热发电、烘干物料。
本发明相对于现有技术具有如下的优点及效果：
1.通过本发明部件的调节功能，可以使系统切换为CO 2自富集型预分解窑或常规在线型预分解窑。虽然水泥行业实施碳减排是大势所趋，但是目前中国对食品级或工业级CO 2产品的市场需求有限。以一条5500t/d规模水泥熟料生产线为例，若将窑尾烟气中CO 2全部捕集提纯为食品级或工业级CO 2产品，则足以满足中国绝大多数CO 2的需求，需要指出的是目前中国不同规模的水泥熟料生产线合计超过1000余条。基于上述考虑，可根据CO 2产品的需求量调节本发明系统的部件，进而灵活调节水泥窑系统CO 2富集量，实现水泥工业碳减排。当对CO 2产品的需求量不高时，水泥窑可 以不进行CO 2自富集，不影响水泥熟料的正常生产；
2.本发明的水泥窑系统无需对回转窑和冷却机等关键烧成设备进行重新设计，即可进行CO 2富集，大大简化工艺流程，降低改造成本，适用于对现有绝大多数预分解窑系统进行改造或新建预分解窑系统的设计；
3.常规预分解窑系统预热器出口烟气量大，CO 2浓度为30％左右，对烟气中CO 2捕集提纯至食品级或工业级浓度时捕集提纯系统的投资成本和运行成本较高。当本发明系统作为CO 2自富集型预分解窑时，第一列旋风预热器和第二列旋风预热器出口烟气中CO 2浓度为30％左右，第三列旋风预热器出口烟气中CO 2浓度＞70％，可大大降低后续CO 2捕集提纯系统投资成本和运行成本，且高CO 2浓度的烟气量可灵活调整为常规预分解窑系统预热器出口烟气量的5～30％，大大降低了预分解窑系统的CO 2排放量。
附图说明
图1是本发明实施例1中由在线型分解炉改造的可调节CO 2富集量的水泥窑图；
图2是本发明实施例2中由在线型分解炉改造的可调节CO 2富集量的水泥窑图；
图3为实施例3中三次风管的局部示意图；
其中，1-A列旋风预热器的进料口，2-B列旋风预热器的进料口，3-C列旋风预热器的进料口，4-分解炉的燃烧器，5-分解炉A，6-第二分料阀，7-第一分料阀，8-分解炉B，9-分解炉B的进风口，10-三次风管，11-回转窑的燃烧器，12-冷却机，13-风机，14-回转窑，15-烟室，16-A列旋风预热器的烟气出口，17-B列旋风预热器的烟气出口，18-C列旋风预热器的烟气出口，19-冷却器，20-冷却器的烟气出口，21-热交换器，2101-气体入口，2102-气体出口。
具体实施方式
为了使本发明的目的、技术方案及优点更加清楚明白，以下结合实施例，对本发明进行进一步详细说明。应当理解，此处所描述的具体实施例仅仅用以解释本发明，并不用于限定本发明。
在本发明的描述中，需要说明的是，除非另有明确的规定和限定，术语“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域的普通技术人员而言，可以具体情况理解上述术语在本发明中的具体含义。
实施例1
如图1所示，可调节CO 2富集量的水泥窑系统包括A列旋风预热器、B列旋风预热器、C列旋风预热器、分解炉A(5)、分解炉B(8)、烟室(15)、回转窑(14)、冷却机(12)；A列旋风预热器、B列旋风预热器的进风口均连接分解炉A(5)，A列旋风预热器、B列旋风预热器的倒数第一级旋风分离器的出料口均连接烟室(15)；C列旋风预热器的进风口连接分解炉B(8)，C列旋风预热器的出料口连接烟室(15)；分解炉A(5)与烟室(15)相连接，烟室(15)连接回转窑(14)；回转窑(14)与冷却机(12)相连接。分解炉A(5)和分解炉B(8)上均设置有分解炉的燃烧器(4)；回转窑(14)上设置有回转窑的燃烧器(11)；冷却机(12)上设置有三次风管(10)；冷却机(12)下方设置有风机(13)。
B列旋风预热器的倒数第二级旋风分离器的下料管处设置有第一分料阀(7)，第一分料阀(7)的一端连分解炉A(5)，第一分料阀(7)的另一端连接分解炉B(8)。
A列旋风预热器的倒数第二级旋风分离器通过管道连接分解炉A(5)，所述管道包含支路，A列旋风预热器对分解炉A(5)多点进料；所述管道包括输送干路和输送支路，输送支路的数量为2个以上，各个输送支路之 间并联，输送干路与输送支路的连接处设置有第二分料阀(6)；第二分料阀(6)的一端连接输送干路，第二分料阀(6)的其他端口连接输送支路；第二分料阀(6)可以调节由输送干路进入输送支路的物料量。
冷却机(12)选自篦式冷却机、单筒冷却机、多筒冷却机中的一种；
A列旋风预热器、B列旋风预热器、C列旋风预热器上均设置有进料口，A列旋风预热器的进料口(1)、B列旋风预热器的进料口(2)、C列旋风预热器的进料口(3)设置在A列旋风预热器、B列旋风预热器、C列旋风预热器的最上面第一级旋风分离器的进口风管处。根据需要，所述进料口也可以设置在A列旋风预热器、B列旋风预热器、C列旋风预热器的最上面第二级旋风分离器的进口风管处。任选地，C列旋风预热器可以设置或不设置进料口。具体地，当C列旋风预热器的级数为2级时，C列旋风预热器的进料口设置在C列旋风预热器的最上面第一级旋风分离器的进口风管处。当C列旋风预热器的级数为3级以上时，C列旋风预热器的进料口设置在C列旋风预热器的最上面第一级旋风分离器的进口风管处，或者设置在C列旋风预热器的最上面第二级旋风分离器的进口风管处。
所述C列旋风预热器与B列旋风预热器之间设置有连通管道，所述连通管道用于将C列旋风预热器预热完成的生料输送至B列旋风预热器。根据需要，可以在C列旋风预热器与A列旋风预热器之间设置有连通管道，和/或C列旋风预热器与B列旋风预热器之间设置有连通管道；所述连通管道用于将C列旋风预热器预热完成的生料输送至A列旋风预热器或B列旋风预热器，或者同时输送至A列旋风预热器和B列旋风预热器。
通过部件的调节，系统可以切换为CO 2自富集型预分解窑或常规在线型预分解窑。具体地，系统可通过部件的调节切换为以下三种情况的任一种。
第一种情况：通过A列旋风预热器的进料口(1)、B列旋风预热器的进料口(2)、C列旋风预热器的进料口(3)将生料喂入到系统中，通过第 一分料阀(7)将B列旋风预热器中的热生料分配至分解炉A(5)和分解炉B(8)，氧气经过分解炉B的进风口(9)进入分解炉B(8)，分解炉B(8)内为全氧燃烧，系统为CO 2自富集型预分解窑。
生料经提升机由喂料装置分别喂入A列、B列和C列旋风预热器，在旋风预热器内实现预热和气固分离。A列生料经过多次换热和气固分离后从A列倒数第二级旋风分离器进入分解炉A(5)。B列生料经过多次换热和气固分离后在第一分料阀(7)内分为两路，其中一路进分解炉A(5)，另外一路进分解炉B(8)。
C列旋风预热器中喂入的生料用于冷却由分解炉B(8)排出的高温烟气。C列旋风预热器预热完成的生料通过连通管道进B列旋风预热器。连通管道的一端设置在C列旋风预热器倒数第二级旋风分离器的出料口，连通管道的另一端设置在B列旋风预热器最上面第一级旋风分离器的进口风管上。根据需要，C列预热完成的生料可以通过连通管道进B列旋风预热器或A列旋风预热器或同时进A列旋风预热器和B列旋风预热器，连通管道进A列旋风预热器或B列旋风预热器的进料点可以设置在A列旋风预热器或B列旋风预热器最上面第一级旋风分离器的进口风管上，或者设置在A列旋风预热器或B列旋风预热器最上面第二级旋风分离器的进口风管上，或者设置在A列旋风预热器或B列旋风预热器最上面第三级旋风分离器的进口风管上，或者设置在A列旋风预热器或B列旋风预热器最上面第四级旋风分离器的进口风管上，或者设置在A列旋风预热器或B列旋风预热器最上面第五级旋风分离器的进口风管上，具体进料点位置可根据实际情况进行调整。
分解炉内燃料燃烧释放大量热量供生料分解，分解完成的热生料离开分解炉A(5)与分解炉B(8)，随后与烟气分离后进入回转窑(14)，在回转窑(14)内煅烧形成熟料，熟料由回转窑(14)出口进入冷却机(12)，随后经冷却机(12)冷却至65℃+环境温度。
需要指出的是，根据预分解窑系统现场布置情况，也可考虑将A列部分预热完成的生料输送至分解炉B(8)内吸热分解，此时可考虑将B列预热完成的全部生料输送至分解炉A(5)内吸热分解。
空气经冷却机(12)对高温熟料进行冷却，换热完成的空气主要分为以下三路：第一路高温空气(900～1200℃)作为二次风直接进入回转窑(14)内供燃料燃烧；第二路高温空气(800～1000℃)作为三次风通过三次风管进入分解炉A(5)内供燃料燃烧；第三路温度较高的空气(250～450℃)可以进入余热锅炉发电或其他余热利用或处理系统，发电完成或其他余热利用或处理系统的烟气通过余风处理后经烟囱排入大气。
经过空气分离装置制得的纯氧进入分解炉B(8)，供进入分解炉B(8)内的燃料燃烧，分解炉B(8)内为全氧燃烧。分解炉B(8)内燃料燃烧和生料分解形成的烟气离开分解炉B(8)进入C列旋风预热器，随后对C列生料进行预热和气固分离，最终从C列旋风预热器出口离开。从C列旋风预热器的烟气出口(18)离开的烟气中CO 2浓度＞70％，烟气温度根据C列旋风预热器设置的旋风分离器级数及C列旋风预热器中生料喂入量等进行控制，通过对该部分烟气进行干燥除尘及CO 2捕集提纯等一系列操作可获得资源化利用的浓度大于99％的CO 2产品。
回转窑(14)内燃料燃烧和部分生料分解形成的窑气进分解炉A(5)，分解炉A(5)内燃料燃烧和生料分解形成的烟气以及来自回转窑(14)的窑气一起离开分解炉A(5)分别进入A列和B列旋风预热器，随后对A列和B列生料进行多次预热和气固分离，最终分别从A列旋风预热器的烟气出口(16)和B列旋风预热器的烟气出口(17)离开。从A列和B列旋风预热器出口离开的烟气中CO 2浓度为30％左右，烟气温度为300～400℃，随后烟气通过窑尾余热锅炉进行发电，进生料磨烘干生料，随后经烟气处理系统处理后排入大气。
通过调节第一分料阀(7)进入分解炉B(8)的热生料量能够调节CO 2 富集量。
第二种情况：系统各部件的调节、物料和气体的流向与第一种情况相同，不同之处在于，将C列旋风预热器出口排出烟气的一部分作为循环烟气，循环烟气与氧气的混合气体通过分解炉B的进风口(9)进入分解炉B(8)，分解炉B(8)内为富氧燃烧，系统为CO 2自富集型预分解窑。
A列旋风预热器出口、B列旋风预热器出口排出的烟气中CO 2浓度为30％左右，C列旋风预热器出口排出的烟气中CO 2浓度＞70％。
通过调节第一分料阀(7)进分解炉B(8)的进料量能够调节CO 2富集量。
第三种情况：生料喂入A列和B列旋风预热器，C列旋风预热器不再喂入生料，此时A列生料和B列生料全部进分解炉A(5)，分解炉B(8)以及C列旋风预热器停止使用，系统为常规在线型预分解窑。
A列旋风预热器出口、B列旋风预热器出口排出的烟气中CO 2浓度为30％左右，烟气温度为300～400℃。
实施例2
如图2所示，系统各部件的连接关系与实施例1相同，不同之处在于，C列旋风预热器的级数为1级，C列旋风预热器的出风口连接冷却器(19)，冷却器(19)用于冷却由C列旋风预热器排出的烟气，冷却后的烟气由冷却器的烟气出口(20)排出。通过对该部分烟气进行干燥除尘及CO 2捕集提纯等一系列操作可获得资源化利用的浓度大于99％的CO 2产品。
通过第一分料阀(7)将B列旋风预热器中的热生料输送至分解炉A(5)和分解炉B(8)，通过第一分料阀(7)可以调节进入分解炉B(8)内的物料量，进而调节CO 2的富集量。
需要指出的是，根据预分解窑系统现场布置情况，也可考虑将A列部分预热完成的生料输送至分解炉B(8)内吸热分解，此时可考虑将B列预热完成的全部生料输送至分解炉A(5)内吸热分解。
通过部件的调节，系统可以切换为CO 2自富集型预分解窑或常规在线型预分解窑。具体地，系统可通过部件的调节切换为以下三种情况的任一种。
第一种情况：通过A列旋风预热器的进料口(1)、B列旋风预热器的进料口(2)将生料喂入到系统中，通过第一分料阀(7)将B列旋风预热器中的热生料分配至分解炉A(5)、分解炉B(8)，氧气通过分解炉B的进风口(9)进入分解炉B(8)，分解炉B(8)内为全氧燃烧，系统为CO 2自富集型预分解窑。
A列旋风预热器出口、B列旋风预热器出口排出的烟气中CO 2浓度为30％左右，C列旋风预热器出口排出的烟气中CO 2浓度>70％。
分解炉B(8)分解完成的生料通过管道进入与其相连的C列旋风分离器进行气固分离，分离后的物料通过管道输送到烟室(15)中，分离后的气体通过管道进入冷却器(19)中进行冷却，冷却完成的烟气中CO 2浓度＞70％。
第二种情况：系统各部件的调节、物料和气体的流向与第一种情况相同，不同之处在于，将由冷却器(19)出口排出烟气的一部分作为循环烟气，循环烟气与氧气的混合气体通过分解炉B的进风口(9)进入分解炉B(8)，分解炉B(8)内为富氧燃烧，系统为CO 2自富集型预分解窑。
A列旋风预热器出口、B列旋风预热器出口排出的烟气中CO 2浓度为30％左右，C列旋风预热器出口排出的烟气中CO 2浓度在>70％。
通过调节第一分料阀(7)进入分解炉B(8)的进料量能够调节CO 2富集量。
第三种情况：生料喂入A列和B列旋风预热器，C列旋风预热器不再喂入生料，此时A列生料和B列生料全部进分解炉A(5)，分解炉B(8)、C列旋风预热器以及冷却器(19)停止使用，系统为常规在线型预分解窑。
A列旋风预热器出口、B列旋风预热器出口排出的烟气中CO 2浓度为 30％左右。
实施例3
如图3所示，冷却机(12)上设置有三次风管(10)，三次风管(10)分为两路，三次风管(10)的一端连接冷却机(12)，其中一路三次风管(10)的另一端连接分解炉A(5)；另一路为三次风管(10)的另一端连接热交换器(21)，热交换器(21)通过管道连接分解炉B(8)。
热交换器(21)上设置有气体入口(2101)、气体出口(2102)。气体出口(2102)连接余热利用或处理系统，所述余热利用或处理系统包括余热发电、烘干物料等。氧气和循环烟气的混合气体或氧气通过气体入口(2101)输送到热交换器(21)内，三次风通过三次风管(10)输送到热交换器(21)内，氧气和循环烟气的混合气体或氧气与三次风在热交换器(21)内进行热量交换。热量交换完成的三次风通过气体出口(2102)进入余热利用或处理系统，热量交换完成的氧气和循环烟气的混合气体或氧气通过管道进入分解炉B(8)。
当氧气输送到热交换器(21)时，三次风在热交换器(21)内对氧气进行预热，预热完成的氧气进入分解炉B(8)，分解炉B(8)内为全氧燃烧。
当氧气和循环烟气的混合气体输送到热交换器(21)时，三次风在热交换器(21)内对氧气和循环烟气的混合气体进行预热，预热完成的氧气和循环烟气的混合气体进入分解炉B(8)，分解炉B(8)内为富氧燃烧。
根据需要，可以将实施例3中的三次风管(10)、热交换器(21)应用到实施例1或实施例2或已知的水泥窑系统中。
以上所述仅为本发明的较佳实施例而已，并不用以限制本发明，凡在本发明的精神和原则之内所作的任何修改、等同替换和改进等，如调整A列、B列或C列旋风预热器级数、调整C列旋风预热器预热完成生料进B 列或A列旋风预热器位置等均应包含在本发明的保护范围之内。

Claims (15)

  1. 由在线型分解炉改造的可调节CO 2富集量水泥窑系统，其特征在于，所述水泥窑系统包括：第一列旋风预热器、第二列旋风预热器、第三列旋风预热器、第一分解炉、第二分解炉、烟室、回转窑、冷却机；
    第一列旋风预热器、第二列旋风预热器的进风口均连接第一分解炉；第一列旋风预热器的出料口或第二列旋风预热器的出料口连接第二分解炉；第三列旋风预热器的进风口连接第二分解炉，第三列旋风预热器的倒数第一级旋风分离器的出料口连接烟室；
    第一分解炉与烟室相连接，烟室连接回转窑；回转窑与冷却机相连接。
  2. 根据权利要求1所述的由在线型分解炉改造的可调节CO 2富集量水泥窑系统，其特征在于，
    第二列旋风预热器的倒数第二级旋风分离器的下料管处设置有第一分料阀，第一分料阀的一端连第一分解炉，第一分料阀的另一端连接第二分解炉。
  3. 根据权利要求1所述的由在线型分解炉改造的可调节CO 2富集量水泥窑系统，其特征在于，第一列旋风预热器的倒数第二级旋风分离器通过管道连接第一分解炉，所述管道不包含支路或包含支路；
    所述管道不包含支路时，第一列旋风预热器对第一分解炉单点进料；
    所述管道包含支路时，第一列旋风预热器对第一分解炉多点进料；所述管道包括输送干路和输送支路，输送支路的数量为2个以上，各个输送支路之间并联，输送干路与输送支路的连接处设置有第二分料阀；第二分料阀用于调节由输送干路进入输送支路的物料量。
  4. 根据权利要求1所述的由在线型分解炉改造的可调节CO 2富集量水泥窑系统，其特征在于，第一列旋风预热器的级数、第二列旋风预热器的级数选自3～7级；
    第三列旋风预热器的级数选自1～5级。
  5. 根据权利要求1所述的由在线型分解炉改造的可调节CO 2富集量水 泥窑系统，其特征在于，冷却机选自篦式冷却机、单筒冷却机、多筒冷却机中的一种；
    所述水泥窑系统还包括三次风管；所述三次风管的一端连接冷却机，所述三次风管的另一端连接第一分解炉。
  6. 根据权利要求1所述的由在线型分解炉改造的可调节CO 2富集量水泥窑系统，其特征在于，所述水泥窑系统还包括冷却器，第三列旋风预热器的出风口连接冷却器；所述冷却器用于冷却由第三列旋风预热器出风口排出的烟气。
  7. 根据权利要求4所述的由在线型分解炉改造的可调节CO 2富集量水泥窑系统，其特征在于，所述第一列旋风预热器、第二列旋风预热器上均设置有进料口，所述进料口设置在第一列旋风预热器、第二列旋风预热器的最上面第一级旋风分离器的进口风管处，或者设置在第一列旋风预热器、第二列旋风预热器的最上面第二级旋风分离器的进口风管处；
    第三列旋风预热器设置或不设置进料口；
    当第三列旋风预热器的级数为1级时，第三列旋风预热器上不设置进料口；
    当第三列旋风预热器的级数为2级以上时，第三列旋风预热器上设置进料口；第三列旋风预热器的进料口设置在第三列旋风预热器的最上面第一级旋风分离器的进口风管处，或者设置在第三列旋风预热器的最上面第二级旋风分离器的进口风管处。
  8. 根据权利要求7所述的由在线型分解炉改造的可调节CO 2富集量水泥窑系统，其特征在于，当所述第三列旋风预热器级数为2级以上时，所述第三列旋风预热器与第一列旋风预热器之间设置有连通管道，和/或第三列旋风预热器与第二列旋风预热器之间设置有连通管道；所述连通管道用于将第三列旋风预热器预热完成的生料输送至第一列旋风预热器或第二列旋风预热器，或者同时输送至第一列旋风预热器和第二列旋风预热器中；
    所述连通管道的一端设置在第三列旋风预热器倒数第二级旋风分离器的出料口处；
    连通管道的另一端设置在第一列旋风预热器或第二列旋风预热器最上面第一级旋风分离器的进口风管上，或者设置在第一列旋风预热器或第二列旋风预热器最上面第二级旋风分离器的进口风管上，或者设置在第一列旋风预热器或第二列旋风预热器最上面第三级旋风分离器的进口风管上，或者设置在第一列旋风预热器或第二列旋风预热器最上面第四级旋风分离器的进口风管上，或者设置在第一列旋风预热器或第二列旋风预热器最上面第五级旋风分离器的进口风管上。
  9. 根据权利要求5所述的由在线型分解炉改造的可调节CO 2富集量水泥窑系统，其特征在于，所述水泥窑系统还包括热交换器，所述三次风管分为两路，三次风管的一端连接冷却机，其中一路为三次风管的另一端连接第一分解炉；另一路为三次风管的另一端连接热交换器，热交换器通过管道连接第二分解炉。
  10. 使用权利要求1-9任一项所述由在线型分解炉改造的可调节CO 2富集量水泥窑系统制备水泥熟料的方法，其特征在于，所述方法包括：
    将生料分别加入第一列旋风预热器、第二列旋风预热器，生料在旋风预热器内与烟气进行换热；
    第一列旋风预热器和第二列旋风预热器预热后的生料通过一点或多点进入第一分解炉；第一列旋风预热器或第二列旋风预热器或第一列旋风预热器和第二列旋风预热器预热后的部分热生料通过一点或多点进入第二分解炉；
    分解完成的热生料离开第一分解炉、第二分解炉，随后与烟气分离后进入回转窑，在回转窑内煅烧形成水泥熟料，熟料由回转窑出口进入冷却机；
    将氧气与循环烟气的混合气体或氧气输送到第二分解炉内，第二分解 炉内为富氧燃烧或全氧燃烧，第二分解炉内产生的高CO 2浓度烟气经第三列旋风预热器排出；通过调节进第二分解炉的热生料量能够调节CO 2富集量。
  11. 根据权利要求10所述的制备水泥熟料的方法，其特征在于，第二列旋风预热器预热后的生料通过第一分料阀分为两路，一路进入第一分解炉，另一路进入第二分解炉；
    通过调节第一分料阀进第二分解炉的热生料量能够调节CO 2富集量。
  12. 根据权利要求11所述的制备水泥熟料的方法，其特征在于，
    将生料分别喂入第一列旋风预热器、第二列旋风预热器，第一列旋风预热器和第二列旋风预热器预热后的生料进入第一分解炉，通过第一分料阀调节向第二分解炉内输送热生料量，第二分解炉内为富氧燃烧或全氧燃烧，此时系统为CO 2自富集型预分解窑，通过调节第一分料阀进第二分解炉的热生料量能够调节CO 2富集量；
    将生料分别喂入第一列旋风预热器、第二列旋风预热器，第一列旋风预热器和第二列旋风预热器预热后的生料进入第一分解炉，调节第一分料阀使第二列旋风预热器预热后的生料全部输送到第一分解炉，第二分解炉、第三列旋风预热器、冷却器停止使用，此时系统为常规在线型预分解窑。
  13. 根据权利要求10所述的制备水泥熟料的方法，其特征在于，生料喂入第三列旋风预热器时，第三列旋风预热器预热后的生料通过连通管道进入第一列旋风预热器或第二列旋风预热器，或者同时进入第一列旋风预热器和第二列旋风预热器。
  14. 根据权利要求10所述的制备水泥熟料的方法，其特征在于，按气体流向而言，空气经冷却机对高温熟料进行冷却，换热完成的空气包括以下三路：第一路高温空气作为二次风直接进入回转窑内供燃料燃烧；第二路高温空气作为三次风直接进入第一分解炉内供燃料燃烧；第三路温度较高的空气进入余热锅炉发电或其他余热利用或处理系统，发电完成或其他 余热利用或处理系统的烟气通过余风处理后经烟囱排入大气。
  15. 根据权利要求14所述的制备水泥熟料的方法，其特征在于，所述第二路高温空气作为三次风分为两路，其中一路三次风通过三次风管进入第一分解炉；另一路三次风通过三次风管进入热交换器，氧气和循环烟气的混合气体或氧气进入热交换器，热量交换完成的氧气和循环烟气的混合气体或氧气通过管道进入第二分解炉，第二分解炉内为富氧燃烧或全氧燃烧；热量交换完成的三次风进入余热利用或处理系统；
    所述余热利用或处理系统包括余热发电、烘干物料。
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