WO2021026714A1 - 一种水泥预分解窑系统及制备水泥熟料的方法 - Google Patents

一种水泥预分解窑系统及制备水泥熟料的方法 Download PDF

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Publication number
WO2021026714A1
WO2021026714A1 PCT/CN2019/100164 CN2019100164W WO2021026714A1 WO 2021026714 A1 WO2021026714 A1 WO 2021026714A1 CN 2019100164 W CN2019100164 W CN 2019100164W WO 2021026714 A1 WO2021026714 A1 WO 2021026714A1
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Prior art keywords
valve
row
decomposition furnace
kiln
oxygen
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PCT/CN2019/100164
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English (en)
French (fr)
Inventor
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/CN2019/100164 priority Critical patent/WO2021026714A1/zh
Priority to CN201980054895.8A priority patent/CN112654828B/zh
Publication of WO2021026714A1 publication Critical patent/WO2021026714A1/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
    • C04B7/24—Cements from oil shales, residues or waste other than slag
    • 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
    • F27B19/04—Combinations of furnaces of kinds not covered by a single preceding main group arranged for associated working
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding

Definitions

  • the invention belongs to the technical field of cement production equipment, and specifically relates to a cement precalcining kiln system and a method for preparing cement clinker.
  • 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 precalcining kiln system, which includes a first row of cyclone preheaters, a second row of cyclone preheaters, a decomposition furnace, a smoke chamber, a rotary kiln, a cooler, and a heat exchanger;
  • the air inlet of the first row of cyclone preheaters is connected to the decomposition furnace, the discharge outlet of the first row of cyclone preheaters is connected to the smoke chamber; the air inlet of the second row of cyclone preheaters is connected to the smoke chamber, and the second row of cyclone preheaters
  • the discharge port is divided into two ways, one is connected to the decomposition furnace, and the other is connected to the smoke chamber;
  • the smoke chamber is connected to the rotary kiln; the rotary kiln is connected to the cooler;
  • the cooling machine is provided with a tertiary air pipe, the tertiary air pipe is divided into two ways by the switching component, one is the tertiary air pipe connected to the heat exchanger, and the heat exchanger is connected to the decomposition furnace through the pipe; the other is the tertiary air pipe without heat exchange The device is directly connected to the decomposition furnace.
  • a distributing valve is provided at the discharge port of the second row of cyclone preheaters, one end of the distributing valve is connected to the decomposition furnace, and the other end of the distributing valve is connected to the smoke chamber.
  • the distributing valve divides the raw material passing through the discharge port of the second row of cyclone preheaters to the decomposition furnace and the smoke chamber; the distributing valve regulates the discharge of the second row of cyclone preheaters The amount of raw meal entering the calciner and smoke chamber.
  • the switching member is selected from valves, such as gate valves or butterfly valves.
  • the valve includes a first valve, a second valve, and a third valve; the first valve and the third valve are arranged on the tertiary air pipe, and the second valve is arranged to connect the heat exchanger and the decomposition On the furnace pipe;
  • the first valve is arranged on the tertiary air pipe connecting the cooler and the heat exchanger
  • the second valve is arranged on the pipe connecting the heat exchanger and the decomposition furnace
  • the third valve is arranged on the tertiary air pipe connecting the cooler and the decomposition furnace .
  • the first valve is valve B
  • the second valve is valve C
  • the third valve is valve A
  • the number of stages of the first row of cyclone preheaters and the second row of cyclone preheaters is selected from 3 to 7.
  • the heat exchanger is provided with more than one gas inlet and more than one gas outlet; one of the gas inlets transports a mixture of oxygen and circulating flue gas or oxygen to the heat exchanger;
  • One of the gas outlets is connected to a waste heat utilization or processing system, the gas outlet conveys the tertiary air that completes heat exchange to the waste heat utilization or processing system;
  • the waste heat utilization or processing system includes a waste heat boiler for power generation, drying materials or other waste heat utilization Or processing device;
  • the cooler is selected from one of grate coolers, single-tube coolers, and multi-tube coolers.
  • the present invention also provides a method for preparing cement clinker using the above cement precalcining kiln system, 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 enters the decomposition furnace through one or more points, and the raw meal preheated by the second row of cyclone preheaters can be divided into two paths, one of which passes through one or more points to enter the decomposition furnace Furnace, the other way enters the rotary kiln through the smoke chamber;
  • the hot raw material decomposed in the calciner leaves the calciner and enters the last cyclone separator of the first row of preheaters. After gas-solid separation, it enters the rotary kiln through the flue chamber, where it is calcined to form mature materials and clinker Enter the cooler from the outlet of the rotary kiln, and then be cooled by the cooler to obtain cement clinker;
  • the kiln gas formed in the rotary kiln passes through the gas-solid heat exchange of the second row of cyclone preheaters and is discharged from the outlet of the top cyclone separator; the flue gas formed in the decomposition furnace passes through the gas of the first row of cyclone preheaters. After solid heat exchange, it is discharged from the outlet of the top cyclone separator;
  • the tertiary air is divided into two ways by the switching part, and any one of the following ways can be selected by adjusting the switching part: one way is the tertiary air enters the heat exchanger through the tertiary air pipe, and the mixed gas or oxygen of the tertiary air and oxygen and circulating flue gas passes through the heat exchanger. Heat exchange, the mixed gas of circulating flue gas and oxygen or oxygen after the heat exchange enters the decomposition furnace, the tertiary air after the heat exchange enters the waste heat utilization or treatment system, and the other way is the tertiary air enters directly through the tertiary air pipe without passing through the heat exchanger. In the decomposition furnace, the hot air in the tertiary duct enters the decomposition furnace.
  • the raw meal feeding point is the inlet pipe of the first cyclone preheater of the first row of cyclone preheaters, the uppermost cyclone separator of the second row of cyclone preheaters, or the first row of cyclone preheating
  • the switching component when the switching component is switched to the tertiary air pipe connected to the heat exchanger, and the heat exchanger is connected to the decomposition furnace through the pipe, the mixed gas of circulating flue gas and oxygen or oxygen passes through the heat exchanger and the heat in the tertiary air pipe.
  • the tertiary air passes through the heat exchanger to heat the circulating flue gas and oxygen mixture gas or oxygen, and the circulating flue gas and oxygen mixture gas or oxygen Entering the decomposition furnace, the decomposition furnace is oxy-fuel combustion or all-oxygen combustion, and the system is a CO 2 self-enriching precalciner;
  • the tertiary air pipe is directly connected to the decomposition furnace, and the hot air in the tertiary air pipe enters the decomposition furnace.
  • the system is an offline precalciner kiln;
  • the first row of cyclone preheaters will no longer feed raw materials, and the fuel in the decomposition furnace will no longer be supplied, and the second row of cyclone preheaters will be put into the second row through the distribution valve
  • the preheated hot raw materials are all distributed into the flue chamber, and then the hot raw materials enter the rotary kiln, where they are calcined to form mature materials.
  • the clinker enters the cooler from the outlet of the rotary kiln, and then is cooled by the cooler to obtain cement cooked materials.
  • the system is a preheater kiln.
  • the tertiary air passes through the heat exchanger to heat the oxygen into the decomposition furnace, and the decomposition furnace is full-oxygen combustion;
  • the tertiary air passes through the heat exchanger to heat the mixed gas of circulating flue gas and oxygen into the decomposition furnace, and the decomposition furnace is oxygen-enriched combustion.
  • the air cools the high-temperature clinker through a cooler, and the air after the heat exchange is divided into the following three paths: the first high-temperature air directly enters the rotary kiln as the secondary air for supply Fuel combustion; when the third valve is fully closed, the first valve and the second valve are fully open, that is, when the system is used as a CO 2 self-enriching precalciner, the second high-temperature air is used as the tertiary air to pass through the heat exchanger to oxygen and The mixed gas or oxygen of the circulating flue gas is preheated, the preheated tertiary air enters the waste heat utilization or treatment system, and the mixed gas or oxygen of the preheated oxygen and the circulating flue gas enters the decomposition furnace; when the third valve is fully opened, When the first and second valves are fully closed, that is, when the system is used as an off-line precalciner, the second high-temperature air is used as tert
  • the air outlet of the cooling machine may be the first, second, or third path; or the first path may be a single outlet, and the second path and the third path may be combined.
  • the combined air outlet of the second road and the third road is that the second road and the third road share one air outlet pipe;
  • the first row of cyclone preheaters will no longer feed raw materials
  • the fuel in the decomposition furnace will no longer be supplied
  • the distribution valve will preheat the second row of cyclone preheaters.
  • the cement precalciner kiln system of the present invention can have different uses of CO 2 self-enrichment precalciner kiln, off-line precalciner kiln or preheater kiln.
  • the CO 2 concentration of the gas discharged from the outlet of the first row of cyclone preheaters is greater than 70%, and the CO 2 concentration of the gas discharged from the outlet of the second row of cyclone preheaters is about 25%;
  • the cement precalciner When the system is switched to an offline precalciner kiln, the cement precalciner will not perform CO 2 self-enrichment.
  • the CO 2 concentration in the flue gas at the outlet of the first cyclone preheater is about 35%, and the second cyclone preheats
  • the CO 2 concentration in the flue gas at the outlet of the device is about 25%.
  • the cement precalciner kiln When the system is switched to a preheater kiln, the cement precalciner kiln does not carry out CO 2 self-enrichment, the first row of cyclone preheaters does not feed raw meal, and the outlet of the first row of cyclone preheaters has no flue gas.
  • the second row of cyclone preheaters are fed, and the CO 2 concentration in the flue gas at the outlet of the second row of cyclone preheaters is about 30%.
  • the first row of cyclone preheaters and the second row of cyclone preheaters include a cyclone separator and a connecting duct; the raw meal undergoes heat exchange and gas-solid separation in the cyclone preheater.
  • the temperature of the material after being cooled by the cooler may be 65° C. + ambient temperature.
  • the temperature of the first air path is 900-1200°C
  • the temperature of the second air path is 800-1000°C;
  • the temperature of the third air is 250-450°C.
  • the fuel combustion environment in the decomposition furnace is oxy-fuel combustion or oxy-fuel combustion, and oxygen can directly enter the decomposition furnace, or oxygen and first Part of the flue gas discharged from the outlet of the cyclone preheater is mixed in a certain proportion and then enters the decomposition furnace.
  • the cement precalciner is used as an offline precalciner, the fuel combustion medium in the precalciner is high temperature tertiary air.
  • part of the flue gas discharged from the outlet of the first row of cyclone preheaters can be mixed into the decomposition furnace as circulating flue gas and oxygen.
  • the temperature at which the raw materials in the calciner decomposes and leaves the calciner is 800-950°C;
  • the oxygen can be prepared by a method known in the art, for example, the oxygen can be obtained by processing air by an air separation system.
  • the mixed gas of circulating flue gas and oxygen or oxygen can also directly enter the decomposition furnace without passing through the heat exchanger.
  • the principle of the present invention is:
  • the mixed gas of oxygen and circulating flue gas or oxygen is sent to the decomposition furnace for fuel combustion in the decomposition furnace to release a large amount of heat.
  • the raw meal added by one row of cyclone preheaters and the second row of cyclone preheaters undergoes multiple heat exchange and separation and then absorbs heat and decomposes in the decomposition furnace to release a large amount of CO 2.
  • the flue gas at the outlet of the decomposition furnace is high-concentration CO 2
  • the flue gas enters the first row of cyclone preheaters through the cyclone separator of the first row of cyclone preheaters.
  • the raw meal in the first row of cyclone preheaters is preheated many times and finally from the first row of cyclones.
  • the outlet of the cyclone separator of the top stage of the preheater leaves.
  • the CO 2 concentration of the flue gas at the outlet of the cyclone separator of the first row of cyclone preheaters is greater than 70%.
  • the formed kiln gas is separated from the raw meal gas and solid in the second row of cyclone preheaters by the cyclone separator of the second row of cyclone preheaters, and the separated flue gas is treated by the second row of cyclone preheaters.
  • the raw meal in the second row is preheated many times, and finally leaves from the exit of the uppermost cyclone separator of the second row of cyclone preheaters.
  • the second row of cyclone preheating The CO 2 concentration of the flue gas at the outlet of the uppermost cyclone separator of the reactor is about 25%, and then the flue gas enters the waste heat utilization or treatment system.
  • the air in the tertiary air duct directly enters the decomposition furnace without passing through the heat exchanger.
  • the first row of cyclone preheaters, decomposition furnaces, and heat exchangers do not work
  • the second row of cyclone preheaters, rotary kilns, and coolers are in normal use
  • the second row of cyclones The CO 2 concentration in the flue gas at the outlet of the preheater is about 30%.
  • the present invention has the following advantages and effects:
  • the present invention creatively integrates the CO 2 self-enriching precalciner kiln, off-line precalciner kiln, and preheater kiln in the same system, and the system can be freely switched to CO 2 self-enriching precalciner, Offline precalciner kiln, preheater kiln.
  • the present invention does not need to redesign the rotary kiln and the cooling machine, and the system of the present invention can be obtained by simple transformation of most existing precalciner kiln systems, which greatly reduces the manufacturing cost.
  • the CO 2 concentration of the flue gas at the outlet of the first row of cyclone preheaters is> 70%
  • the CO 2 concentration of the flue gas at the outlet of the second row of cyclone preheaters is 25
  • the flue gas volume is only about 35% of the flue gas volume at the outlet of the preheater of the existing precalciner kiln system, which greatly reduces the CO 2 emission of the precalciner kiln system.
  • the CO 2 concentration of the flue gas at the outlet of the first row of cyclone preheaters and the second row of cyclone preheaters is about 25% to 35%.
  • the system is switched to a preheater kiln, it can meet the needs of online maintenance of a series of cyclone preheaters.
  • the fuel combustion medium in the rotary kiln is air, and there is a large amount of N 2 in the combustion products.
  • the entrance of the rotary kiln is connected with the bottom of the calciner, so the presence of N 2 in the kiln gas will inevitably greatly reduce the flue gas in the calciner
  • the concentration of CO 2 is not convenient for subsequent purification and purification of CO 2 in the flue gas at the outlet of the cyclone preheater.
  • the inlet of the rotary kiln is connected with the connecting air pipe of the lowest stage of the second row of cyclone separators.
  • the kiln gas performs multiple preheating and gas-solid separation of the raw meal passing through the second row of cyclone separators without entering the decomposition furnace Therefore, it has no effect on the CO 2 concentration of the flue gas in the decomposition furnace, and the problem of low CO 2 concentration of the kiln tail flue gas in the prior art and difficult purification and purification is improved.
  • Figure 1 is a system diagram of a cement precalcining kiln in an embodiment of the present invention.
  • the raw meal feed inlet of column 1-A cyclone preheater the raw meal feed inlet of column 2-B cyclone preheater, 3-calciner, 4-fuel inlet of calciner, 5-distribution valve, 6 -Smoke chamber, 7-rotary kiln, 8-tertiary duct, 9-fuel inlet of the rotary kiln, 10-cooler, 11-valve B, 12-valve C, 13-valve A, 14-heat exchanger, 1401 -Gas inlet, 1402-gas outlet, 15-A column cyclone preheater flue gas outlet, 16-B column cyclone preheater flue gas outlet, 17-fan.
  • 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 precalcining kiln system includes column A cyclone preheater, column B cyclone preheater, decomposition furnace (3), smoke chamber (6), rotary kiln (7), cooler (10), Heat exchanger (14); the air inlet of the cyclone preheater of column A is connected to the decomposition furnace (3); the air inlet of the cyclone preheater of column B is connected to the smoke chamber (6), and the outlet of the cyclone preheater of column B A distributing valve (5) is arranged, one end of the distributing valve (5) is connected with the decomposition furnace (3), and the other end of the distributing valve (5) is connected with the smoke chamber (6).
  • the smoke chamber (6) is connected to the rotary kiln (7); the rotary kiln (7) is connected to the cooler (10); the cooler (10) is provided with a tertiary air pipe (8), and the tertiary air pipe (8) is divided into Two routes, one is the tertiary air pipe (8) connected to the heat exchanger (14), the heat exchanger (14) is connected to the decomposition furnace (3) through a pipe; the other is the tertiary air pipe directly connected without passing through the heat exchanger (14) Decomposing furnace (3); the valve includes valve B (11), valve C (12), valve A (13); the valve B (11) and valve A (13) are arranged on the tertiary air pipe (8) , The valve C (12) is set on the pipe connecting the heat exchanger (14) and the decomposition furnace (3); the valve B (11) is set on the tertiary air pipe () connecting the cooler (10) and the heat exchanger (14) 8), valve C (12) is set on the pipe connecting the heat exchanger (14)
  • the distributing valve (5) divides the raw meal passing through the discharge port of the B-row cyclone preheater to the decomposition furnace (3) and the smoke chamber (6); the distributing valve (5) is regulated by the B-row cyclone preheater The amount of raw meal entering the decomposition furnace (3) and the smoke chamber (6) from the discharge port.
  • the calciner (3) is provided with fuel inlets (4) of the calciner, and the number of fuel inlets (4) of the calciner can be more than one, for example, four.
  • the rotary kiln (7) is provided with a fuel inlet (9) of the rotary kiln.
  • the valve can be selected from gate valve or butterfly valve, etc.;
  • the heat exchanger (14) is provided with more than one gas inlet and more than one gas outlet; wherein the gas outlet (1402) is connected to a waste heat utilization or processing system; the waste heat utilization or processing system includes a waste heat boiler for power generation and drying Dry materials or other devices for waste heat utilization or processing; a mixture of oxygen and circulating flue gas or oxygen can be passed into the heat exchanger (14) through the gas inlet (1401).
  • the cooler is selected from one of grate coolers, single-tube coolers, and multi-tube coolers.
  • valve B (11), valve C (12), valve A (13), and distribution valve (5), the system can be switched to any of the following four situations:
  • valve A (13) is fully closed
  • valve B (11) and valve C (12) are fully open
  • the cement precalciner kiln system is used as a CO 2 self-enrichment type precalciner.
  • the raw meal is fed into the column A cyclone preheater and column B cyclone preheater from the raw meal feed inlet (1) of the cyclone preheater column A and the raw meal feed inlet (2) of the cyclone preheater column B respectively.
  • the raw meal can be preheated to 700 ⁇ 800°C through the cyclone separator and the connecting air pipe for multiple heat exchanges with the flue gas; the preheated raw meal of column A enters the decomposition furnace from the penultimate cyclone of column A (3), the preheated raw meal in column B is divided into two paths through the distribution valve (5), one of which enters the decomposition furnace (3) and the other one enters the smoke chamber (6).
  • the fuel enters the calciner (3) through the fuel inlet (4) of the calciner.
  • the fuel burns in the calciner (3) and releases a large amount of heat for the decomposition of the raw meal.
  • the hot raw meal after the decomposition leaves the calciner (3) through the bottom of the column A
  • the first-stage cyclone separator enters the rotary kiln (7) after gas-solid separation.
  • the mature material is calcined in the rotary kiln (7).
  • the clinker enters the cooler (10) from the outlet of the rotary kiln (7), and then passes through the cooler (10).
  • the flue gas produced by fuel combustion and raw meal decomposition in the decomposition furnace (3) enters the lowermost cyclone separator of column A from the outlet of the decomposition furnace (3), and completes the gas solidification with the hot raw material After separation, it enters the penultimate cyclone separator of column A, and preheats the raw meal of column A in the cyclone separator and the connecting air pipe many times, and finally leaves from the outlet of the top cyclone separator of column A.
  • the temperature of the flue gas discharged from the flue gas outlet (15) of the cyclone preheater of column A is 300-400°C, and the CO 2 concentration in the flue gas is greater than 70%. After purification, drying, capture and purification, etc., the purity of more than 99% can be obtained. CO 2 , and then proceed to resource treatment or storage.
  • the air at ambient temperature cools the high-temperature clinker entering from the outlet of the rotary kiln (7) by the cooler (10).
  • the air after the heat exchange is divided into three paths: the first air enters the rotary kiln (7) as High temperature secondary air (900 ⁇ 1200°C) for fuel combustion.
  • the second high-temperature air (800 ⁇ 1000°C) enters the tertiary air pipe (8) as tertiary air, the oxygen enters the heat exchanger (14) through the gas inlet (1401), and the tertiary air passes through the heat exchanger (14) to preheat the oxygen.
  • the preheated oxygen enters the decomposition furnace (3) through a pipe, and the decomposition furnace (3) is full-oxygen combustion, and the preheated tertiary air enters the waste heat utilization or treatment system.
  • the third air (250-450°C) enters the waste heat boiler for power generation or other waste heat utilization or treatment system, and the air from the power generation or other waste heat utilization or treatment system passes through the waste air treatment system and is discharged into the atmosphere through the chimney.
  • the kiln gas formed by the combustion of fuel and the decomposition of a small amount of raw meal is separated from the gas and solid of the raw meal in the row B by the cyclone separator at the bottom of row B, and the separated flue gas is treated by the cyclone preheater in row B.
  • the raw meal in column B is preheated several times, and finally leaves from the flue gas outlet (16) of the cyclone preheater in column B; the temperature of the flue gas at the outlet of the cyclone preheater in column B is 300 ⁇ 400°C, and the CO 2 concentration in the flue gas is 25
  • the flue gas from the power generation or other waste heat utilization or treatment system passes through the waste air treatment system and is discharged into the atmosphere through the chimney.
  • valve A (13) is fully closed, valve B (11) and valve C (12) are fully opened, and the cement precalciner kiln is used as a CO 2 self-enriching precalciner.
  • the difference from the first case is that part of the flue gas discharged from the flue gas outlet (15) of the cyclone preheater of column A is used as the circulating flue gas, and the mixed gas of the circulating flue gas and oxygen is passed through the gas inlet (1401 ) Is transported to the heat exchanger (14), the tertiary air and the mixed gas exchange heat in the heat exchanger (14), the mixed gas after the heat exchange is transported to the decomposition furnace (3) through the pipeline, the decomposition furnace (3) Inside is oxy-fuel combustion.
  • valve A (13) is fully opened, valve B (11) and valve C (12) are fully closed, and the cement precalciner is used as an offline precalciner.
  • the flow direction of the material in the system is the same as the first and second cases above, and the flow direction of the gas is different from the first and second cases above.
  • the air at ambient temperature cools the high-temperature clinker entering from the outlet of the rotary kiln (7) by the cooler (10).
  • the air after the heat exchange is divided into three paths: the first air enters the rotary kiln (7) as High-temperature secondary air (900-1200°C) for fuel combustion, the second air enters the tertiary air pipe (8) as tertiary air (800-1000°C), and the tertiary air directly enters the decomposition furnace (3) for fuel combustion.
  • the third air (250 ⁇ 450°C) enters the waste heat boiler for power generation or other waste heat utilization or treatment system.
  • the air from the power generation or other waste heat utilization or treatment system passes through the waste air treatment system and is discharged into the atmosphere through the chimney.
  • the kiln gas formed by the combustion of fuel and the decomposition of a small amount of raw meal is separated from the gas and solid of the raw meal in the row B by the cyclone separator at the bottom of row B, and the separated flue gas is treated by the cyclone preheater in row B.
  • the raw meal in column B is preheated many times, and finally leaves from the flue gas outlet (16) of the cyclone preheater in column B.
  • the flue gas formed in the decomposition furnace is discharged from the flue gas outlet (15) of the A cyclone preheater through the cyclone preheater of column A, and the flue gas formed in the rotary kiln is preheated by the cyclone of column B through the cyclone preheater of column B
  • the flue gas outlet (16) of the device is discharged.
  • the temperature of the flue gas discharged from the flue gas outlet (15) of the cyclone preheater of column A and the flue gas outlet (16) of the cyclone preheater of column B is 300 ⁇ 400°C, and the flue gas outlet of the cyclone preheater of column A ( 15)
  • the CO 2 concentration in the discharged flue gas is about 35%, and the CO 2 concentration in the flue gas discharged from the flue gas outlet (16) of the column B cyclone preheater is about 25%.
  • valve A (13), valve B (11), valve C (12) are fully closed, the distribution valve (5) distributes all the preheated hot raw materials to the smoke chamber (6), cement
  • the precalciner kiln system acts as a preheater kiln.
  • the cyclone preheater of column A no longer feeds raw meal, and the outlet of column A has no smoke; the raw meal is fed through the raw meal feed inlet (2) of the cyclone preheater of column B, and the raw meal is fed through the cyclone separator and the connecting duct Exchanging heat with flue gas for many times, the final raw meal can be preheated to 700 ⁇ 800°C; all the preheated hot raw meal is distributed to the smoke chamber (6) through the distribution valve (5), and then sent to the rotary kiln (7).
  • the hot raw material is calcined in the rotary kiln (7) to form mature material, and the clinker enters the cooler (10) from the outlet of the rotary kiln (7), and then is cooled to 65°C + ambient temperature by the cooler (10).
  • the air at ambient temperature cools the high-temperature clinker falling from the outlet of the rotary kiln by the cooler (10).
  • the air after the heat exchange is divided into two paths: the first air enters the rotary kiln and serves as high temperature for fuel combustion Secondary air (900 ⁇ 1200°C).
  • the second path of air enters the waste heat boiler for power generation or other waste heat utilization or treatment system, and the air from the power generation or other waste heat utilization or treatment system passes through the waste air treatment system and is discharged into the atmosphere through the chimney; among them, in the rotary kiln ( 7)
  • the kiln gas formed by internal fuel combustion and the decomposition of a small amount of raw meal is separated from the raw meal of row B by the bottom cyclone separator of row B, and the separated flue gas is passed through the cyclone preheater of row B to the raw meal of row B.
  • the flue gas temperature of the flue gas outlet (16) of the cyclone preheater in column B is 300 ⁇ 400°C, and the CO in the flue gas 2
  • the concentration is about 30%, and then the flue gas enters the waste heat boiler for power generation or other waste heat utilization or treatment system, and the flue gas from the power generation or other waste heat utilization or treatment system passes through the waste air treatment system and is discharged into the atmosphere through the chimney.

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Abstract

一种水泥预分解窑系统及制备水泥熟料的方法。将CO 2自富集型预分解窑、离线型预分解窑、预热器窑集于同一系统，可根据需要将系统切换为CO 2自富集型预分解窑、离线型预分解窑或预热器窑。极大降低了烟气中CO 2捕集提纯的投资和运行成本，为水泥行业实现碳减排提供有效的解决方案。而且，系统无需对回转窑（7）和冷却机（10）进行重新设计，大大降低制造成本。当系统切换为预热器窑时，可满足一列旋风预热器在线检修的需要。另外，改善了现有技术中窑尾烟气CO 2浓度低、净化提纯成本高的问题。

Description

一种水泥预分解窑系统及制备水泥熟料的方法 技术领域
本发明属于水泥生产设备技术领域，具体涉及一种水泥预分解窑系统及制备水泥熟料的方法。
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年全国水泥熟料产量接近19亿吨，在现有技术水平下，每生产1吨水泥熟料的CO 2排放量约为0.84吨，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。目前水泥行业可采用的碳减排技术方案为燃烧前捕集、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。
因此，亟需研发一种系统简单、设备投资小、运行成本低且具有富集CO 2功能的水泥预分解窑系统。
发明内容
为改善上述缺陷，本发明提供一种水泥预分解窑系统，包括第一列旋风预热器、第二列旋风预热器、分解炉、烟室、回转窑、冷却机、热交换器；
第一列旋风预热器的进风口连接分解炉，第一列旋风预热器的出料口连接烟室；第二列旋风预热器的进风口连接烟室，第二列旋风预热器的出料口分为两路，一路连接分解炉，另一路与烟室相连接；
烟室连接回转窑；回转窑与冷却机连接；
冷却机上设置有三次风管，所述三次风管通过切换部件分为两路，一路是三次风管连接热交换器，热交换器通过管道连接分解炉；另一路是三次风管不经热交换器直接连接分解炉。
根据本发明的实施方案，第二列旋风预热器的出料口处设置分料阀，分料阀的一端与分解炉相连接，分料阀的另一端与烟室相连接。
根据本发明的实施方案，分料阀将经过第二列旋风预热器出料口的生料分至分解炉、烟室；所述分料阀调节由第二列旋风预热器的出料口进入分解炉、烟室的生料量。
根据本发明的实施方案，所述切换部件选自阀门，例如闸板阀或蝶阀 等。
根据本发明的实施方案，所述阀门包括第一阀门、第二阀门、第三阀门；所述第一阀门、第三阀门设置在三次风管上，第二阀门设置在连接热交换器与分解炉的管道上；
第一阀门设置在连接冷却机与热交换器的三次风管上，第二阀门设置在连接热交换器与分解炉的管道上；第三阀门设置在连接冷却机与分解炉的三次风管上。
根据本发明的实施方案，所述第一阀门为阀门B，所述第二阀门为阀门C，所述第三阀门为阀门A。
根据本发明的实施方案，所述第一列旋风预热器、第二列旋风预热器的级数选自3～7级。
根据本发明的实施方案，所述热交换器上设置有一个以上的气体入口、一个以上的气体出口；其中一个气体入口将氧气与循环烟气的混合气体或氧气输送至热交换器；
其中一个气体出口连接余热利用或处理系统，所述气体出口将完成热量交换的三次风输送至余热利用或处理系统；所述余热利用或处理系统包括余热锅炉发电、烘干物料或其他进行余热利用或处理的装置；
所述冷却机选自篦式冷却机、单筒冷却机、多筒冷却机中的一种。
本发明还提供使用上述水泥预分解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；
第一列旋风预热器预热后的生料通过一点或多点进入分解炉，第二列 旋风预热器预热后的生料可分为两路，其中一路通过一点或多点进入分解炉，另外一路通过烟室进入回转窑；
分解炉内分解完成的热生料离开分解炉进入第一列预热器的最后一级旋风分离器，经过气固分离后通过烟室进入回转窑，在回转窑内煅烧形成熟料，熟料由回转窑出口进入冷却机，随后经冷却机冷却，得到水泥熟料；
回转窑内形成的窑气经第二列旋风预热器的气固换热后由最上面一级旋风分离器的出口排出；分解炉内形成的烟气经第一列旋风预热器的气固换热后由最上面一级旋风分离器的出口排出；
三次风通过切换部件分为两路，通过调节切换部件选择以下任意一路：一路是三次风通过三次风管进入热交换器，三次风与氧气与循环烟气的混合气体或氧气通过热交换器进行热量交换，热量交换完成的循环烟气和氧气的混合气体或氧气进入分解炉，热量交换完成的三次风进入余热利用或处理系统，另一路是三次风通过三次风管不经热交换器直接进入分解炉，三次风管内的热空气进入分解炉。
根据本发明的实施方案，生料喂入点为第一列旋风预热器、第二列旋风预热器的最上面第一级旋风分离器的进风管，或者为第一列旋风预热器、第二列旋风预热器最上面第二级旋风分离器的进风管。
根据本发明的实施方案，当切换部件转换至三次风管连接热交换器，热交换器通过管道连接分解炉时，循环烟气和氧气的混合气体或氧气通过热交换器与三次风管内的热空气进行热量交换，热量交换完成的三次风进入余热利用或处理系统，热量交换完成的循环烟气和氧气的混合气体或氧气进入分解炉，分解炉内为富氧燃烧或全氧燃烧。
根据本发明的实施方案，第三阀门关闭、第一阀门和第二阀门打开时， 三次风经过热交换器加热循环烟气和氧气的混合气体或氧气，循环烟气和氧气的混合气体或氧气进入分解炉，分解炉内为富氧燃烧或全氧燃烧，此时所述系统为CO 2自富集型预分解窑；
第三阀门打开、第一阀门和第二阀门关闭时，三次风管直接连接分解炉，三次风管内的热空气进入分解炉，此时所述系统为离线型预分解窑；
第一阀门、第二阀门、第三阀门均关闭时，第一列旋风预热器不再喂入生料，分解炉内燃料不再供应，通过分料阀将第二列旋风预热器中预热完成的热生料全部分配到烟室中，随后热生料进入回转窑，在回转窑内煅烧形成熟料，熟料由回转窑出口进入冷却机，随后经冷却机冷却，得到水泥熟料，此时所述系统为预热器窑。
根据本发明的实施方案，第三阀门关闭、第一阀门和第二阀门打开时，三次风经过热交换器加热氧气进入分解炉，分解炉内为全氧燃烧；
第三阀门关闭、第一阀门和第二阀门打开时，三次风经过热交换器加热循环烟气和氧气的混合气体进入分解炉，分解炉内为富氧燃烧。
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，换热完成的空气分为以下三路：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；当第三阀门全关，第一阀门和第二阀门全开时，即系统作为CO 2自富集型预分解窑时，第二路高温空气作为三次风通过热交换器对氧气与循环烟气的混合气或氧气进行预热，预热完成的三次风进余热利用或处理系统，预热完成的氧气与循环烟气的混合气或氧气进分解炉；当第三阀门全开，第一阀门和第二阀门全关时，即系统作为离线型预分解窑时，第二路高温空气作为三次风直接进分解炉内供燃料燃烧，分解炉内不再供入氧气与循环烟气的混合气体或氧气；第三路空气进入余 热利用或处理系统。
进一步地，冷却机的出风可以为第一路、第二路、第三路；或为第一路单独出风，第二路和第三路组合出风。
进一步地，所述第二路和第三路组合出风为第二路和第三路共用一个出风管；
第一阀门、第二阀门、第三阀门均关闭时，第一列旋风预热器不再喂入生料，分解炉内燃料不再供应，分料阀将第二列旋风预热器中预热完成的热生料全部分配到烟室中时，即系统作为预热器窑时，第一路单独出风，第二路和第三路组合出风。
根据切换部件的转换和调节分料阀，本发明的水泥预分解窑系统可以具有CO 2自富集型预分解窑、离线型预分解窑或预热器窑不同用途，当系统切换为CO 2自富集型预分解窑时，第一列旋风预热器出口排出的气体CO 2浓度大于70％，第二列旋风预热器出口排出的气体CO 2浓度为25％左右；
当系统切换为离线型预分解窑时，此时水泥预分解窑不进行CO 2自富集，第一列旋风预热器出口烟气中CO 2浓度为35％左右，第二列旋风预热器出口烟气中CO 2浓度为25％左右。
当系统切换为预热器窑时，水泥预分解窑不进行CO 2自富集，第一列旋风预热器不喂入生料，第一列旋风预热器出口无烟气，生料从第二列旋风预热器喂入，第二列旋风预热器出口烟气中CO 2浓度为30％左右。
根据本发明的实施方案，所述第一列旋风预热器、第二列旋风预热器包括旋风分离器、连接风管；生料在旋风预热器内进行换热和气固分离。
根据本发明的实施方案，经冷却机冷却后的物料温度可以为65℃+环境温度。
根据本发明的实施方案，所述第一路空气的温度为900～1200℃；
所述第二路空气的温度为800～1000℃；
所述第三路空气的温度为250～450℃。
根据本发明的实施方案，当所述系统作为CO 2自富集型预分解窑时，分解炉内燃料燃烧环境为全氧燃烧或富氧燃烧，氧气可以直接进入分解炉，或者氧气与第一列旋风预热器出口排出的部分烟气按一定比例混合后进入分解炉。当水泥预分解窑作为离线型预分解窑时，分解炉内燃料燃烧介质为高温三次风。煤粉燃烧和生料分解在分解炉内释放出大量CO 2，随后分解炉内燃料燃烧和生料分解形成的烟气离开分解炉进入第一列旋风预热器，随后对第一列生料进行多次预热和气固分离，最终从第一列旋风预热器出口离开。
任选地，可以将第一列旋风预热器出口排出的烟气的一部分作为循环烟气与氧气混合进分解炉。
所述分解炉内生料受热分解离开分解炉的温度为800～950℃；
所述氧气可通过本领域的已知方法进行制备，例如，可以通过空气分离系统对空气处理而分离获得氧气。
根据本发明的实施方案，循环烟气与氧气的混合气体或氧气也可以不经过热交换器直接进入分解炉。
本发明的原理为：
在工艺过程中，当水泥预分解窑系统作为CO 2自富集型预分解窑时，氧气与循环烟气的混合气体或氧气送入分解炉，供分解炉内燃料燃烧释放大量热量，由第一列旋风预热器和第二列旋风预热器加入的生料经多次换 热和分离后在分解炉内吸热分解释放出大量CO 2，分解炉出口烟气为高浓度CO 2的烟气，经第一列旋风预热器的最下一级旋风分离器进入第一列旋风预热器，对第一列旋风预热器中的生料多次预热最后从第一列旋风预热器最上一级旋风分离器出口离开，在保证第一列旋风预热器密封性能的前提下，第一列旋风预热器最上一级旋风分离器出口烟气CO 2浓度大于70％，即CO 2自富集过程；任选地，由第一列旋风预热器出口排出的一部分烟气可以作为循环烟气，与氧气混合进入分解炉；在回转窑内燃料燃烧和少量生料分解形成的窑气经第二列旋风预热器最下一级旋风分离器与第二列旋风预热器中的生料气固分离，分离完成的烟气经第二列旋风预热器对第二列生料进行多次预热，最后从第二列旋风预热器的最上一级旋风分离器出口离开，在保证第二列旋风预热器密封性能的前提下，第二列旋风预热器的最上一级旋风分离器出口烟气CO 2浓度为25％左右，而后烟气进入余热利用或处理系统。
当水泥预分解窑系统作为离线型预分解窑时，三次风管中的空气不经热交换器直接进入分解炉内。
当水泥预分解窑系统作为预热器窑时，第一列旋风预热器、分解炉、热交换器不工作，第二列旋风预热器、回转窑、冷却机正常使用，第二列旋风预热器出口烟气中CO 2浓度为30％左右。
本发明相对于现有技术具有如下的优点及效果：
1.本发明创造性地将CO 2自富集型预分解窑、离线型预分解窑、预热器窑集于同一系统，可根据需要将系统自由切换为CO 2自富集型预分解窑、离线型预分解窑、预热器窑。
2.当系统切换为CO 2自富集型预分解窑时，在分解炉内可实现CO 2自富集过程，第一列旋风预热器出口烟气CO 2浓度＞70％，极大降低了后续烟气中CO 2捕集提纯的投资成本和运行成本。
3.本发明无需对回转窑和冷却机进行重新设计，对现有大多数预分解窑系统进行简单改造即可得到本发明系统，大大降低了制造成本。
4.本发明系统切换为CO 2自富集型预分解窑时，第一列旋风预热器出口烟气CO 2浓度＞70％，第二列旋风预热器出口烟气CO 2浓度为25％左右，且烟气量仅为现有预分解窑系统预热器出口烟气量的35％左右，大大降低了预分解窑系统的CO 2排放量。本发明系统切换为离线型预分解窑时，第一列旋风预热器、第二列旋风预热器出口烟气CO 2浓度为25％～35％左右。当系统切换为预热器窑时，可满足一列旋风预热器在线检修的需要。
5.现有技术中，回转窑内燃料燃烧介质为空气，燃烧产物中存在大量N 2，回转窑入口与分解炉底部相连，这样窑气中N 2的存在必然会大幅降低分解炉内烟气CO 2的浓度，也不便于后续旋风预热器出口烟气中CO 2的净化提纯。本发明将回转窑入口与第二列旋风分离器的最下一级连接风管相连，窑气对经过第二列旋风分离器的生料进行多次预热和气固分离，不会进入分解炉，所以对分解炉内烟气CO 2浓度没有影响，改善了现有技术中窑尾烟气CO 2浓度低，净化提纯困难的问题。
附图说明
图1是本发明实施例中水泥预分解窑系统图。其中，1-A列旋风预热器的生料喂入口，2-B列旋风预热器的生料喂入口，3-分解炉，4-分解炉的燃料入口，5-分料阀，6-烟室，7-回转窑，8-三次风管，9-回转窑的燃料入口，10-冷却机，11-阀B，12-阀C，13-阀A，14-热交换器，1401-气体入口，1402- 气体出口，15-A列旋风预热器的烟气出口，16-B列旋风预热器的烟气出口，17-风机。
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。
如图1所示，水泥预分解窑系统包括A列旋风预热器、B列旋风预热器、分解炉(3)、烟室(6)、回转窑(7)、冷却机(10)、热交换器(14)；A列旋风预热器的进风口连接分解炉(3)；B列旋风预热器的进风口连接烟室(6)，B列旋风预热器的出料口处设置分料阀(5)，分料阀(5)的一端与分解炉(3)相连接，分料阀(5)的另一端与烟室(6)相连接。烟室(6)连接回转窑(7)；回转窑(7)与冷却机(10)连接；冷却机(10)上设置有三次风管(8)，三次风管(8)通过阀门分为两路，一路是三次风管(8)连接热交换器(14)，热交换器(14)通过管道连接分解炉(3)；另一路是三次风管不经过热交换器(14)直接连接分解炉(3)；所述阀门包括阀B(11)、阀C(12)、阀A(13)；所述阀B(11)、阀A(13)设置在三次风管(8)上，阀C(12)设置在连接热交换器(14)与分解炉 (3)的管道上；阀B(11)设置在连接冷却机(10)与热交换器(14)的三次风管(8)上，阀C(12)设置在连接热交换器(14)与分解炉(3)的管道上；阀A(13)设置在连接冷却机(10)与分解炉(3)的三次风管(8)上。分料阀(5)将经过B列旋风预热器出料口的生料分至分解炉(3)、烟室(6)；所述分料阀(5)调节由B列旋风预热器的出料口进入分解炉(3)、烟室(6)的生料量。分解炉(3)上设置有分解炉的燃料入口(4)，分解炉的燃料入口(4)的数量可以为1个以上，例如4个。回转窑(7)上设置有回转窑的燃料入口(9)。
所述阀门可以选自闸板阀或蝶阀等；
所述热交换器(14)上设置有一个以上的气体入口、一个以上的气体出口；其中，气体出口(1402)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锅炉发电、烘干物料或其他进行余热利用或处理的装置；可以通过气体入口(1401)向热交换器(14)中通入氧气与循环烟气的混合气体或氧气。
所述冷却机选自篦式冷却机、单筒冷却机、多筒冷却机中的一种。
通过阀B(11)、阀C(12)、阀A(13)、分料阀(5)的切换，可以将系统切换为以下四种情况的任一种：
第一种情况：阀A(13)全关，阀B(11)和阀C(12)全开，水泥预分解窑系统作为CO 2自富集型预分解窑。
生料分别从A列旋风预热器的生料喂入口(1)和B列旋风预热器的生料喂入口(2)喂入A列旋风预热器和B列旋风预热器，生料经旋风分离器和连接风管与烟气多次换热，最终生料可预热至700～800℃；预热完成的A列生料从A列倒数第二级旋风分离器进入分解炉(3)，预热完成的B列生 料通过分料阀(5)分为两路，其中一路进分解炉(3)，另外一路进烟室(6)。燃料经分解炉的燃料入口(4)进入分解炉(3)，分解炉(3)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(3)经A列最下一级旋风分离器气固分离后进入回转窑(7)，在回转窑(7)内煅烧形成熟料，熟料由回转窑(7)出口进入冷却机(10)，随后经冷却机(10)冷却至65℃+环境温度；分解炉(3)内燃料燃烧和生料分解产生的烟气从分解炉(3)出口进入A列最下一级旋风分离器，与热生料完成气固分离后进入A列倒数第二级旋风分离器，在旋风分离器和连接风管内对A列生料进行多次预热，最终从A列最上一级旋风分离器出口离开。
A列旋风预热器的烟气出口(15)排出的烟气温度为300～400℃，烟气中CO 2浓度大于70％，经过净化干燥和捕集提纯等工艺可得到99％以上纯度的CO 2，然后进行资源化处理或封存。环境温度下的空气经冷却机(10)对从回转窑(7)出口进入的高温熟料进行冷却，换热完成后的空气分为三路：第一路空气进入回转窑(7)内作为供燃料燃烧的高温二次风(900～1200℃)。第二路高温空气(800～1000℃)作为三次风进入三次风管(8)，氧气通过气体入口(1401)进入热交换器(14)，三次风通过热交换器(14)对氧气进行预热，预热完成的氧气通过管道进入分解炉(3)，分解炉(3)内为全氧燃烧，预热完成的三次风进入余热利用或处理系统。第三路空气(250～450℃)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、处理系统的空气通过余风处理系统后经烟囱排入大气。
在回转窑(7)内燃料燃烧和少量生料分解形成的窑气经B列最下一级旋风分离器与B列生料气固分离，分离完成的烟气经B列旋风预热器对B列生料进行多次预热，最后从B列旋风预热器的烟气出口(16)离开；B 列旋风预热器出口烟气温度300～400℃，烟气中CO 2浓度为25％左右，随后烟气进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、处理系统的烟气通过余风处理系统后经烟囱排入大气。
第二种情况：阀A(13)全关，阀B(11)和阀C(12)全开，水泥预分解窑作为CO 2自富集型预分解窑。
与第一种情况的不同之处在于：将A列旋风预热器的烟气出口(15)排出的烟气的一部分作为循环烟气，将循环烟气与氧气的混合气体通过气体入口(1401)输送到热交换器(14)内，三次风与混合气体在热交换器(14)内进行热量交换，热量交换完成的混合气体通过管道输送到分解炉(3)内，分解炉(3)内为富氧燃烧。
第三种情况：阀A(13)全开，阀B(11)和阀C(12)全关，水泥预分解窑作为离线型预分解窑。
此时系统内物料的流向与上述第一种情况、第二种情况相同，气体的流向与上述第一种情况、第二种情况不同。
环境温度下的空气经冷却机(10)对从回转窑(7)出口进入的高温熟料进行冷却，换热完成后的空气分为三路：第一路空气进入回转窑(7)内作为供燃料燃烧的高温二次风(900～1200℃)，第二路空气作为三次风(800～1000℃)进入三次风管(8)，三次风直接进分解炉(3)内供燃料燃烧。第三路空气(250～450℃)进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、处理系统的空气通过余风处理系统后经烟囱排入大气。
在回转窑(7)内燃料燃烧和少量生料分解形成的窑气经B列最下一级旋风分离器与B列生料气固分离，分离完成的烟气经B列旋风预热器对B 列生料进行多次预热，最后从B列旋风预热器的烟气出口(16)离开。
分解炉内形成的烟气经A列旋风预热器由A列旋风预热器的烟气出口(15)排出，回转窑内形成的烟气经B列旋风预热器由B列旋风预热器的烟气出口(16)排出。由A列旋风预热器的烟气出口(15)、B列旋风预热器的烟气出口(16)排出的烟气温度300～400℃，由A列旋风预热器的烟气出口(15)排出的烟气中CO 2浓度为35％左右，由B列旋风预热器的烟气出口(16)排出的烟气中CO 2浓度为25％左右。随后烟气进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、处理系统的烟气通过余风处理系统后经烟囱排入大气。
第四种情况：阀A(13)、阀B(11)、阀C(12)全关，分料阀(5)将预热完成的热生料全部分配至烟室(6)中，水泥预分解窑系统作为预热器窑。
A列旋风预热器不再喂入生料，A列出口无烟气；生料经B列旋风预热器的生料喂入口(2)喂入，生料经旋风分离器和连接风管与烟气多次换热，最终生料可预热至700～800℃；通过分料阀(5)将预热完成的热生料全部分配至烟室(6)中，随后输送到回转窑(7)。热生料在回转窑(7)内煅烧形成熟料，熟料由回转窑(7)出口进入冷却机(10)，随后经冷却机(10)冷却至65℃+环境温度。
环境温度下的空气经冷却机(10)对从回转窑出口落入的高温熟料进行冷却，换热完成的空气分为两路：第一路空气进入回转窑内，作为供燃料燃烧的高温二次风(900～1200℃)。第二路空气(250～1000℃)进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、处理系统的空气通过余风处理系统后经烟囱排入大气；其中，在回转窑(7)内燃料燃 烧和少量生料分解形成的窑气经B列最下一级旋风分离器与B列生料气固分离，分离完成的烟气经B列旋风预热器对B列生料进行多次预热，最后从B列旋风预热器的烟气出口(16)离开；B列旋风预热器的烟气出口(16)排出的烟气温度300～400℃，烟气中CO 2浓度为30％左右，随后烟气进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、处理系统的烟气通过余风处理系统后经烟囱排入大气。
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列和B列旋风预热器级数、O2与循环烟气的混合比例、B列生料进回转窑部位等均应包含在本发明的保护范围之内。

Claims (16)

  1. 一种水泥预分解窑系统，其特征在于，
    所述系统包括第一列旋风预热器、第二列旋风预热器、分解炉、烟室、回转窑、冷却机、热交换器；
    第一列旋风预热器的进风口连接分解炉，第一列旋风预热器的出料口连接烟室；第二列旋风预热器的进风口连接烟室，第二列旋风预热器的出料口分为两路，一路连接分解炉，另一路与烟室相连接；
    烟室连接回转窑；回转窑与冷却机连接；
    冷却机上设置有三次风管，所述三次风管通过切换部件分为两路，一路是三次风管连接热交换器，热交换器通过管道连接分解炉；另一路是三次风管不经过热交换器直接连接分解炉。
  2. 根据权利要求1所述的水泥预分解窑系统，其特征在于，第二列旋风预热器的出料口处设置分料阀，分料阀的一端与分解炉相连接，分料阀的另一端与烟室相连接。
  3. 根据权利要求1或2所述的水泥预分解窑系统，其特征在于，分料阀将经过第二列旋风预热器出料口的生料分至分解炉、烟室；所述分料阀调节由第二列旋风预热器的出料口进入分解炉、烟室的生料量。
  4. 根据权利要求1所述的水泥预分解窑系统，其特征在于，所述切换部件选自阀门。
  5. 根据权利要求4所述的水泥预分解窑系统，其特征在于，所述阀门选自闸板阀或蝶阀。
  6. 根据权利要求4所述的水泥预分解窑系统，其特征在于，
    所述阀门包括第一阀门、第二阀门、第三阀门；所述第一阀门、第三阀门设置在三次风管上，第二阀门设置在连接热交换器与分解炉的管道上；
    第一阀门设置在连接冷却机与热交换器的三次风管上，第二阀门设置在连接热交换器与分解炉的管道上；第三阀门设置在连接冷却机与分解炉的三次风管上。
  7. 根据权利要求1所述的水泥预分解窑系统，其特征在于，所述第一列旋风预热器、第二列旋风预热器的级数选自3～7级。
  8. 根据权利要求1所述的水泥预分解窑系统，其特征在于，所述热交换器上设置有一个以上的气体入口、一个以上的气体出口；
    其中一个气体出口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锅炉发电、烘干物料；
    所述冷却机选自篦式冷却机、单筒冷却机、多筒冷却机中的一种。
  9. 使用权利要求1-8任一项所述水泥预分解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；
    第一列旋风预热器预热后的生料通过一点或多点进入分解炉，第二列旋风预热器预热后的生料可分为两路，其中一路通过一点或多点进入分解炉，另外一路通过烟室进入回转窑；
    分解炉内分解完成的热生料离开分解炉进入第一列旋风预热器的最后一级旋风分离器，经过气固分离后通过烟室进入回转窑，在回转窑内煅烧形成熟料，熟料由回转窑出口进入冷却机，随后经冷却机冷却，得到水泥熟料；
    回转窑内形成的窑气经第二列旋风预热器气固换热后由最上面一级旋风分离器的出口排出；分解炉内形成的烟气经第一列旋风预热器气固换热 后由最上面一级旋风分离器的出口排出；
    三次风通过切换部件分为两路，通过调节切换部件选择以下任意一路：一路是三次风通过三次风管进入热交换器，三次风与氧气与循环烟气的混合气体或氧气通过热交换器进行热量交换，热量交换完成的循环烟气和氧气的混合气体或氧气进入分解炉，热量交换完成的三次风进入余热利用或处理系统，另一路是三次风通过三次风管不经热交换器直接进入分解炉，三次风管内的热空气进入分解炉。
  10. 根据权利要求9所述的制备水泥熟料的方法，其特征在于，生料喂入点为第一列旋风预热器、第二列旋风预热器最上面一级旋风分离器的进风管，或者为第一列旋风预热器、第二列旋风预热器最上面第二级旋风分离器的进风管。
  11. 根据权利要求9所述的制备水泥熟料的方法，其特征在于，当切换部件转换至三次风管连接热交换器，热交换器通过管道连接分解炉时，循环烟气和氧气的混合气体或氧气通过热交换器与三次风管内的热空气进行热量交换，热量交换完成的三次风进入余热利用或处理系统，热量交换完成的循环烟气和氧气的混合气体或氧气进入分解炉，分解炉内为富氧燃烧或全氧燃烧。
  12. 根据权利要求9所述的制备水泥熟料的方法，其特征在于，第三阀门关闭、第一阀门和第二阀门打开时，三次风经过热交换器加热循环烟气和氧气的混合气体或氧气，循环烟气和氧气的混合气体或氧气进入分解炉，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；
    第三阀门打开、第一阀门和第二阀门关闭时，三次风管直接连接分解炉，三次风管内的热空气进入分解炉，此时系统为离线型预分解窑；
    第一阀门、第二阀门、第三阀门均关闭时，第一列旋风预热器不再喂入生料，分解炉内燃料不再供应，分料阀将第二列旋风预热器中预热完成的热生料全部分配到烟室中时，热生料进入回转窑，在回转窑内煅烧形成熟料，熟料由回转窑出口进入冷却机，随后经冷却机冷却，得到水泥熟料，此时所述系统为预热器窑。
  13. 根据权利要求12所述的制备水泥熟料的方法，其特征在于，第三阀门关闭、第一阀门和第二阀门打开时，三次风经过热交换器加热氧气进入分解炉，分解炉内为全氧燃烧；
    第三阀门关闭、第一阀门和第二阀门打开时，三次风经过热交换器加热循环烟气和氧气的混合气体进入分解炉，分解炉内为富氧燃烧。
  14. 根据权利要求9-13任一项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，换热完成的空气分为以下三路：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；当第三阀门全关，第一阀门和第二阀门全开时，即系统作为CO 2自富集型预分解窑时，第二路高温空气作为三次风通过热交换器对循环烟气和氧气的混合气体或氧气进行预热，预热完成的三次风进余热利用或处理系统，预热完成的循环烟气和氧气的混合气体或氧气进分解炉；当第三阀门全开，第一阀门和第二阀门全关时，即系统作为离线型预分解窑时，第二路高温空气作为三次风直接进分解炉内供燃料燃烧，分解炉内不再供入氧气或氧气与循环烟气的混合气体；第三路空气进入余热利用或处理系统。
  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，冷却机的出风为第一路、第二路、第三路；或为第一路单独出风，第二路和第三路组合出风。
  16. 根据权利要求15所述的制备水泥熟料的方法，其特征在于，所述第二路和第三路组合出风为第二路和第三路共用一个出风管；
    第一阀门、第二阀门、第三阀门均关闭时，第一列旋风预热器不再喂入生料，分解炉内燃料不再供应，分料阀将第二列旋风预热器中预热完成的热生料全部分配到烟室中时，即系统作为预热器窑时，第一路单独出风，第二路和第三路组合出风。
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