CN112654828B - Cement predecomposition kiln system and method for preparing cement clinker - Google Patents
Cement predecomposition kiln system and method for preparing cement clinker Download PDFInfo
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- CN112654828B CN112654828B CN201980054895.8A CN201980054895A CN112654828B CN 112654828 B CN112654828 B CN 112654828B CN 201980054895 A CN201980054895 A CN 201980054895A CN 112654828 B CN112654828 B CN 112654828B
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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
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- 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
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- 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
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Abstract
A cement predecomposition kiln system and a method for preparing cement clinker. CO is introduced into2The self-enrichment type pre-decomposition kiln, the separation line type pre-decomposition kiln and the preheater kiln are integrated in the same system, and the system can be switched into CO according to the requirement2Self-enrichment type pre-decomposition kiln, offline type pre-decomposition kiln or preheater kiln. Greatly reduces CO in the flue gas2The investment and the operation cost of purification are collected, and an effective solution is provided for realizing carbon emission reduction in the cement industry. Moreover, the system does not need to redesign the rotary kiln (7) and the cooler (10), thereby greatly reducing the manufacturing cost. When the system is switched to a preheater kiln, the on-line maintenance requirement of the cyclone preheater in a row can be met. In addition, the kiln tail flue gas CO in the prior art is improved2Low concentration and high purification cost.
Description
Technical Field
The invention belongs to the technical field of cement production equipment, and particularly relates to a cement precalciner system and a method for preparing cement clinker.
Background
CO, a major greenhouse gas2The global greenhouse effect is aggravated by a large amount of emission, and countries in the world are generally confronted with a difficult task of realizing carbon emission reduction and relieving global climate change. In order to better develop global economy and protect natural environment, countries in the world set the strategic targets of carbon emission reduction. In China, the cement industry has becomeSecond largest CO of the electric power industry2A source of emissions. Statistically, the national cement clinker yield in 2018 is close to 19 hundred million tons, and under the state of the art, the yield of CO is 1 ton of cement clinker per production2The emission is about 0.84 ton of CO2Emissions have reached 15.96 million tons in 2018. Therefore, the high CO in the cement industry is slowed down2The discharge problem is not very slow.
Researches on carbon emission reduction technologies have been reported at home and abroad, but the researches mainly face the industries such as electric power, coal, steel and the like, and relatively few reports on the carbon emission reduction technologies related to the cement industry are reported. The carbon emission reduction technical scheme adopted by the cement industry at present is capture before combustion and capture after combustion. Wherein the pre-combustion capture refers to the pretreatment of the fuel before combustion to separate out carbon in the fuel. Due to the characteristics of cement clinker production process, CO before combustion2A significant disadvantage of capture is that only CO produced by combustion of the fuel can be separated2And about 60% of CO produced by calcination of the raw meal2Along with the emission of flue gas, the CO of the part is discharged2No treatment was obtained. Furthermore, pre-combustion capture technology compares to other CO2The capture technology clinker calcination process is very harsh on hydrogen combustion conditions, and a rotary kiln combustor needs to be specially designed, so that the technology has low feasibility in the cement industry and can be eliminated. The capture technology after combustion in cement industry mainly refers to capture or separate CO from flue gas after combustion2The main techniques include absorption, adsorption, membrane absorption, and mineral carbonization. Because the pressure of the tail gas of the cement industrial kiln is small, the volume flow is large, and CO is generated2Low concentration, and contains a large amount of dust and N2The methods have the problems of low carbon capture efficiency, small capture flow, complex system, large equipment investment or high operation cost.
Therefore, it is urgently needed to develop a system which is simple, has low equipment investment and low operation cost and can enrich CO2A functional cement predecomposition kiln system.
Disclosure of Invention
In order to improve the defects, the invention provides a cement precalciner system which comprises a first row of cyclone preheaters, a second row of cyclone preheaters, a decomposing furnace, a smoke chamber, a rotary kiln, a cooler and a heat exchanger, wherein the first row of cyclone preheaters is connected with the second row of cyclone preheaters;
an air inlet of the first row of cyclone preheaters is connected with the decomposing furnace, and a discharge port of the first row of cyclone preheaters is connected with the smoke chamber; the air inlet of the second row of cyclone preheaters is connected with the smoke chamber, the discharge hole of the second row of cyclone preheaters is divided into two paths, one path is connected with the decomposing furnace, and the other path is connected with the smoke chamber;
the smoke chamber is connected with the rotary kiln; the rotary kiln is connected with a cooler;
the cooler is provided with a tertiary air pipe, the tertiary air pipe is divided into two paths through a switching part, one path is that the tertiary air pipe is connected with a heat exchanger, and the heat exchanger is connected with the decomposing furnace through a pipeline; the other path is that the tertiary air pipe is directly connected with the decomposing furnace without a heat exchanger.
According to the embodiment of the invention, a material distributing valve is arranged at the discharge port of the second row of cyclone preheaters, one end of the material distributing valve is connected with the decomposing furnace, and the other end of the material distributing valve is connected with the smoke chamber.
According to the embodiment of the invention, the material distributing valve distributes the raw materials passing through the discharge port of the second row of cyclone preheater to the decomposing furnace and the smoke chamber; the feed divider adjusts the raw material amount entering the decomposing furnace and the smoke chamber from the discharge port of the second row of cyclone preheaters.
According to an embodiment of the invention, the switching member is selected from a valve, such as a gate valve or a butterfly valve, etc.
According to an embodiment of the invention, the valve comprises a first valve, a second valve, a third valve; the first valve and the third valve are arranged on the tertiary air pipe, and the second valve is arranged on a pipeline connecting the heat exchanger and the decomposing furnace;
the first valve is arranged on a tertiary air pipe connecting the cooler and the heat exchanger, and the second valve is arranged on a pipeline connecting the heat exchanger and the decomposing furnace; the third valve is arranged on a tertiary air pipe which connects the cooler and the decomposing furnace.
According to an embodiment of the invention, the first valve is valve B, the second valve is valve C and the third valve is valve a.
According to the embodiment of the invention, the number of the first row of cyclone preheaters and the second row of cyclone preheaters is 3-7.
According to the embodiment of the invention, more than one gas inlet and more than one gas outlet are arranged on the heat exchanger; one of the gas inlets conveys the mixed gas of oxygen and circulating flue gas or oxygen to the heat exchanger;
one of the gas outlets is connected with a waste heat utilization or treatment system, and the gas outlet conveys tertiary air which completes heat exchange to the waste heat utilization or treatment system; the waste heat utilization or treatment system comprises a waste heat boiler for power generation, material drying or other devices for waste heat utilization or treatment;
the cooler is selected from one of a grate cooler, a single-cylinder cooler and a multi-cylinder cooler.
The invention also provides a method for preparing cement clinker by using the cement predecomposition kiln system, which comprises the following steps:
adding the raw materials into a first row of cyclone preheaters and a second row of cyclone preheaters respectively, and exchanging heat between the raw materials and the flue gas in the cyclone preheaters;
the raw materials preheated by the first row of cyclone preheaters enter the decomposing furnace through one point or multiple points, the raw materials preheated by the second row of cyclone preheaters can be divided into two paths, wherein one path enters the decomposing furnace through one point or multiple points, and the other path enters the rotary kiln through the smoke chamber;
the hot raw materials decomposed in the decomposing furnace leave the decomposing furnace and enter a last-stage cyclone separator of a first-stage preheater, the hot raw materials enter a rotary kiln through a smoke chamber after gas-solid separation, the raw materials are calcined in the rotary kiln to form clinker, the clinker enters a cooling machine from an outlet of the rotary kiln and is cooled by the cooling machine, and cement clinker is obtained;
kiln gas formed in the rotary kiln is subjected to gas-solid heat exchange of a second row of cyclone preheaters and then is discharged from an outlet of the uppermost stage of cyclone separator; the flue gas formed in the decomposing furnace is subjected to gas-solid heat exchange by the first row of cyclone preheaters and then is discharged from the outlet of the uppermost stage of cyclone separator;
the tertiary air is divided into two paths by the switching component, and any one of the following paths is selected by adjusting the switching component: one path of the waste heat utilization system is that tertiary air enters a heat exchanger through a tertiary air pipe, the tertiary air and the mixed gas of oxygen and circulating flue gas or the oxygen carry out heat exchange through the heat exchanger, the mixed gas of the circulating flue gas and the oxygen or the oxygen which are subjected to heat exchange enter a decomposing furnace, the tertiary air which is subjected to heat exchange enters a waste heat utilization or treatment system, the other path of the waste heat utilization system is that the tertiary air directly enters the decomposing furnace through the tertiary air pipe without passing through the heat exchanger, and hot air in the tertiary air pipe enters the decomposing furnace.
According to an embodiment of the invention, the raw meal feed point is the air inlet duct of the uppermost first stage cyclone of the first row of cyclone preheaters, of the second row of cyclone preheaters or the air inlet duct of the uppermost second stage cyclone of the first row of cyclone preheaters, of the second row of cyclone preheaters.
According to the embodiment of the invention, when the switching part is switched to the tertiary air pipe to be connected with the heat exchanger which is connected with the decomposing furnace through the pipeline, the mixed gas of the circulating flue gas and the oxygen or the oxygen is subjected to heat exchange with hot air in the tertiary air pipe through the heat exchanger, the tertiary air after the heat exchange is fed into the waste heat utilizing or treating system, the mixed gas of the circulating flue gas and the oxygen or the oxygen after the heat exchange is fed into the decomposing furnace, and the decomposing furnace is subjected to oxygen-enriched combustion or total oxygen combustion.
According to the embodiment of the invention, when the third valve is closed and the first valve and the second valve are opened, the tertiary air passes through the heat exchanger to heat the mixed gas or oxygen of the circulating flue gas and the oxygen, the mixed gas or oxygen of the circulating flue gas and the oxygen enters the decomposing furnace, and the oxygen-enriched combustion or the total oxygen combustion is performed in the decomposing furnace, wherein the system is CO2A self-enrichment type pre-decomposition kiln;
when the third valve is opened and the first valve and the second valve are closed, the tertiary air pipe is directly connected with the decomposing furnace, hot air in the tertiary air pipe enters the decomposing furnace, and the system is an off-line type pre-decomposing kiln;
when the first valve, the second valve and the third valve are all closed, the first row of cyclone preheaters do not feed raw materials, the fuel in the decomposing furnace is not supplied any more, the hot raw materials preheated in the second row of cyclone preheaters are all distributed into the smoke chamber through the material distributing valve, then the hot raw materials enter the rotary kiln and are calcined in the rotary kiln to form clinker, the clinker enters a cooler from the outlet of the rotary kiln and is cooled by the cooler to obtain cement clinker, and at the moment, the system is a preheater kiln.
According to the embodiment of the invention, when the third valve is closed and the first valve and the second valve are opened, the tertiary air passes through the heat exchanger to heat oxygen and enters the decomposing furnace, and the decomposing furnace is in full-oxygen combustion;
when the third valve is closed and the first valve and the second valve are opened, the tertiary air heats the mixed gas of the circulating flue gas and the oxygen through the heat exchanger and enters the decomposing furnace, and the oxygen-enriched combustion is performed in the decomposing furnace.
According to the embodiment of the invention, the air cools the high-temperature clinker through the cooler according to the gas flow direction, and the air after heat exchange is divided into the following three paths: the first path of high-temperature air is used as secondary air and directly enters the rotary kiln for fuel combustion; when the third valve is fully closed and the first valve and the second valve are fully opened, the system is used as CO2When the self-enrichment type pre-decomposition kiln is used, the second path of high-temperature air is used as tertiary air to preheat the mixed gas of oxygen and circulating flue gas or oxygen through a heat exchanger, the preheated tertiary air enters a waste heat utilization or treatment system, and the preheated mixed gas of oxygen and circulating flue gas or oxygen enters a decomposition furnace; when the third valve is fully opened and the first valve and the second valve are fully closed, namely the system is used as an offline pre-decomposition kiln, the second path of high-temperature air is directly fed into the decomposition furnace as tertiary air for fuel combustion, and mixed gas or oxygen of oxygen and circulating flue gas is not fed into the decomposition furnace any more; and the third path of air enters a waste heat utilization or treatment system.
Furthermore, the air outlet of the cooler can be a first path, a second path and a third path; or the first path independently exhausts air, and the second path and the third path are combined to exhaust air.
Further, the combined air outlet of the second path and the third path is an air outlet pipe shared by the second path and the third path;
when the first valve, the second valve and the third valve are all closed, the first row of cyclone preheaters do not feed raw materials, the fuel in the decomposing furnace is not supplied any more, and when the material distributing valve distributes all the hot raw materials preheated in the second row of cyclone preheaters into the smoke chamber, namely when the system is used as a preheater kiln, the first path independently exhausts air, and the second path and the third path combine to exhaust air.
The cement precalciner system of the invention may have a CO predissociation kiln system according to the switching of the switching means and the adjustment of the distribution valve2The self-enrichment type pre-decomposition kiln, the separation line type pre-decomposition kiln or the preheater kiln can be used for different purposes when the system is switched to CO2When the kiln is self-enriched, the gas CO discharged from the outlet of the first cyclone preheater2The concentration of the gas CO is more than 70 percent, and the gas CO is discharged from the outlet of the second row of cyclone preheaters2The concentration is about 25%;
when the system is switched to the linear pre-decomposition kiln, the cement pre-decomposition kiln does not carry out CO2Self-enriching CO in flue gas at outlet of first-row cyclone preheater2The concentration is about 35 percent, and CO is contained in the flue gas at the outlet of the second row of cyclone preheaters2The concentration is about 25%.
When the system is switched to the preheater kiln, the cement predecomposition kiln does not carry out CO2Self-enriching, the first row of cyclone preheaters do not feed raw meal, the outlet of the first row of cyclone preheaters does not have smoke, the raw meal is fed from the second row of cyclone preheaters, and CO in the smoke at the outlet of the second row of cyclone preheaters2The concentration is about 30%.
According to the embodiment of the invention, the first row of cyclone preheaters and the second row of cyclone preheaters comprise cyclone separators and connecting air pipes; the raw meal is subjected to heat exchange and gas-solid separation in the cyclone preheater.
According to an embodiment of the invention, the temperature of the material after cooling by the cooler may be 65 ℃ + ambient temperature.
According to the embodiment of the invention, the temperature of the first path of air is 900-1200 ℃;
the temperature of the second path of air is 800-1000 ℃;
the temperature of the third path of air is 250-450 ℃.
According to an embodiment of the present inventionThe system is used as CO2When the self-enrichment type pre-decomposition kiln is used, the fuel combustion environment in the decomposition furnace is oxy-fuel combustion or oxygen-enriched combustion, oxygen can directly enter the decomposition furnace, or oxygen and part of smoke discharged from the outlet of the first row of cyclone preheaters are mixed according to a certain proportion and then enter the decomposition furnace. When the cement predecomposition kiln is used as the separation line type predecomposition kiln, the fuel combustion medium in the decomposing furnace is high-temperature tertiary air. The combustion of coal powder and the decomposition of raw materials release a large amount of CO in the decomposing furnace2And then the flue gas formed by fuel combustion and raw meal decomposition in the decomposing furnace leaves the decomposing furnace and enters the first row of cyclone preheaters, and then the raw meal in the first row is subjected to multiple preheating and gas-solid separation and finally leaves from the outlet of the first row of cyclone preheaters.
Optionally, a portion of the flue gas exiting the outlet of the first train of cyclone preheaters may be mixed with oxygen as recycle flue gas into the decomposing furnace.
The temperature of the raw material in the decomposing furnace after being heated and decomposed and leaving the decomposing furnace is 800-950 ℃;
the oxygen may be produced by methods known in the art, for example, by processing air through an air separation system to separate the oxygen.
According to the embodiment of the present invention, the mixed gas of the circulating flue gas and oxygen or oxygen may be directly introduced into the decomposing furnace without passing through a heat exchanger.
The principle of the invention is as follows:
in the technical process, when the cement precalciner system is used as CO2When the self-enrichment type pre-decomposition kiln is used, the mixed gas of oxygen and circulating flue gas or oxygen is fed into the decomposing furnace to make the fuel in the decomposing furnace burn and release a large amount of heat, and the raw material added by first row of cyclone preheaters and second row of cyclone preheaters is undergone the processes of several heat exchanges and separation, and then is undergone the process of heat absorption decomposition in the decomposing furnace to release a large amount of CO2The flue gas at the outlet of the decomposing furnace is high-concentration CO2The smoke enters the first row of cyclone preheaters through the lowest stage cyclone separator of the first row of cyclone preheaters, preheats the raw materials in the first row of cyclone preheaters for multiple times, and finally leaves from the outlet of the highest stage cyclone separator of the first row of cyclone preheaters, so that the density of the first row of cyclone preheaters is ensuredOn the premise of sealing performance, the flue gas CO at the outlet of the uppermost stage cyclone separator of the first row of cyclone preheaters2At a concentration of more than 70%, i.e. CO2A self-enrichment process; optionally, a part of the flue gas discharged from the outlet of the first row of cyclone preheaters can be used as circulating flue gas and mixed with oxygen to enter the decomposing furnace; kiln gas formed by combustion of fuel and decomposition of a small amount of raw materials in the rotary kiln is subjected to gas-solid separation with raw materials in a second row of cyclone preheaters through a lowest cyclone separator of the second row of cyclone preheaters, separated flue gas is subjected to multiple preheating on the second row of raw materials through the second row of cyclone preheaters and finally leaves from an outlet of a highest cyclone separator of the second row of cyclone preheaters, and flue gas CO at the outlet of the highest cyclone separator of the second row of cyclone preheaters is separated on the premise of ensuring the sealing performance of the second row of cyclone preheaters2The concentration is about 25%, and then the flue gas enters a waste heat utilization or treatment system.
When the cement predecomposition kiln system is used as an isolated linear predecomposition kiln, air in the tertiary air pipe directly enters the decomposing furnace without passing through a heat exchanger.
When the cement predecomposition kiln system is used as a preheater kiln, the first row of cyclone preheaters, the decomposing furnace and the heat exchanger do not work, the second row of cyclone preheaters, the rotary kiln and the cooler are normally used, and CO in smoke gas at the outlet of the second row of cyclone preheaters2The concentration is about 30%.
Compared with the prior art, the invention has the following advantages and effects:
1. the invention creatively converts CO2The self-enrichment type pre-decomposition kiln, the separation line type pre-decomposition kiln and the pre-heater kiln are integrated in the same system, and the system can be freely switched into CO according to the requirement2Self-enrichment type pre-decomposition kiln, separation line type pre-decomposition kiln and preheater kiln.
2. When the system switches to CO2When the self-enrichment type pre-decomposition kiln is used, CO can be realized in the decomposition furnace2Self-enrichment process, flue gas CO at outlet of first-row cyclone preheater2The concentration is more than 70 percent, and the CO in the subsequent flue gas is greatly reduced2The investment cost and the operation cost of the purification are captured.
3. The system can be obtained by simply modifying most of the existing precalciner systems without redesigning the rotary kiln and the cooler, so that the manufacturing cost is greatly reduced.
4. The system of the invention is switched to CO2When the self-enrichment type pre-decomposition kiln is used, the flue gas CO at the outlet of the first cyclone preheater2The concentration is more than 70 percent, and the flue gas CO at the outlet of the second row of cyclone preheaters2The concentration is about 25 percent, and the smoke volume is only about 35 percent of the smoke volume at the outlet of the preheater of the prior precalciner kiln system, thereby greatly reducing the CO of the precalciner kiln system2And (4) discharging the amount. When the system is switched to the linear separation pre-decomposition kiln, the flue gas CO at the outlets of the first row of cyclone preheaters and the second row of cyclone preheaters2The concentration is about 25 to 35 percent. When the system is switched to a preheater kiln, the on-line maintenance requirement of a row of cyclone preheaters can be met.
5. In the prior art, the fuel combustion medium in the rotary kiln is air, and a large amount of N exists in combustion products2The inlet of the rotary kiln is connected with the bottom of the decomposing furnace, so that N is contained in kiln gas2The existence of the catalyst can inevitably and greatly reduce the flue gas CO in the decomposing furnace2The concentration of the CO in the flue gas at the outlet of the subsequent cyclone preheater is not convenient2Purifying. The inlet of the rotary kiln is connected with the lowest stage connecting air pipe of the second row of cyclone separators, the kiln gas preheats the raw materials passing through the second row of cyclone separators for multiple times and separates gas from solid, and the raw materials cannot enter the decomposing furnace, so that the flue gas CO in the decomposing furnace is treated2The concentration is not influenced, and the kiln tail flue gas CO in the prior art is improved2Low concentration and difficult purification.
Drawings
FIG. 1 is a diagram of a cement precalciner kiln system in an embodiment of the invention. The system comprises a raw material feeding port of a cyclone preheater in 1-A column, a raw material feeding port of a cyclone preheater in 2-B column, a decomposing furnace in 3-4-fuel inlet of the decomposing furnace, a material distributing valve in 5-6-smoke chamber in 7-rotary kiln, a tertiary air pipe in 8-9-fuel inlet of the rotary kiln, a cooling machine in 10-heat exchanger in 11-valve B, a valve C in 12-valve C, a valve A in 13-valve A, a heat exchanger in 14-1401-gas inlet, a gas outlet in 1402-gas outlet, a flue gas outlet of the cyclone preheater in 15-A column, a flue gas outlet of the cyclone preheater in 16-B column and a fan in 17-17.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail with reference to the following embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected" and "connected" are to be interpreted broadly, e.g., as being fixed or detachable or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
As shown in figure 1, the cement pre-decomposition kiln system comprises a cyclone preheater A, a cyclone preheater B, a decomposing furnace (3), a smoke chamber (6), a rotary kiln (7), a cooler (10) and a heat exchanger (14); the air inlet of the A-row cyclone preheater is connected with a decomposing furnace (3); the air inlet of the B-row cyclone preheater is connected with the smoke chamber (6), the discharge port of the B-row cyclone preheater is provided with a material distributing valve (5), one end of the material distributing valve (5) is connected with the decomposing furnace (3), and the other end of the material distributing valve (5) is connected with the smoke chamber (6). The smoke chamber (6) is connected with the rotary kiln (7); the rotary kiln (7) is connected with a cooler (10); a tertiary air pipe (8) is arranged on the cooler (10), the tertiary air pipe (8) is divided into two paths through a valve, one path is that the tertiary air pipe (8) is connected with a heat exchanger (14), and the heat exchanger (14) is connected with the decomposing furnace (3) through a pipeline; the other path is that the tertiary air pipe is directly connected with the decomposing furnace (3) without passing through the heat exchanger (14); the valve comprises a valve B (11), a valve C (12) and a valve A (13); the valve B (11) and the valve A (13) are arranged on the tertiary air pipe (8), and the valve C (12) is arranged on a pipeline connecting the heat exchanger (14) with the decomposing furnace (3); the valve B (11) is arranged on a tertiary air pipe (8) connecting the cooler (10) and the heat exchanger (14), and the valve C (12) is arranged on a pipeline connecting the heat exchanger (14) and the decomposing furnace (3); the valve A (13) is arranged on a tertiary air pipe (8) which is connected with the cooler (10) and the decomposing furnace (3). The material distributing valve (5) distributes the raw materials passing through the discharge port of the cyclone preheater in the row B to the decomposing furnace (3) and the smoke chamber (6); the material distributing valve (5) regulates the amount of raw materials entering the decomposing furnace (3) and the smoke chamber (6) from the discharge hole of the B-row cyclone preheater. The decomposing furnace (3) is provided with a fuel inlet (4) of the decomposing furnace, and the number of the fuel inlets (4) of the decomposing furnace can be more than 1, for example, 4. The rotary kiln (7) is provided with a fuel inlet (9) of the rotary kiln.
The valve can be selected from a gate valve, a butterfly valve and the like;
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 with a waste heat utilization or treatment system; the waste heat utilization or treatment system comprises a waste heat boiler for power generation, material drying or other devices for waste heat utilization or treatment; a mixed gas of oxygen and circulating flue gas or oxygen can be introduced into the heat exchanger (14) through the gas inlet (1401).
The cooler is selected from one of a grate cooler, a single-cylinder cooler and a multi-cylinder cooler.
By switching the valve B (11), the valve C (12), the valve A (13) and the material distributing valve (5), the system can be switched to any one of the following four conditions:
in the first case: valve A (13) is fully closed, valve B (11) and valve C (12) are fully opened, and the cement predecomposition kiln system is used as CO2Self-enrichment type pre-decomposition kiln.
Raw materials are respectively fed into the cyclone preheater A and the cyclone preheater B from a raw material feeding inlet (1) of the cyclone preheater A and a raw material feeding inlet (2) of the cyclone preheater B, the raw materials are subjected to multiple heat exchange with flue gas through a cyclone separator and a connecting air pipe, and finally the raw materials can be preheated to 700-800 ℃; the preheated raw materials in the row A enter the decomposing furnace (3) from the last-but-one secondary cyclone separator in the row A, and the preheated raw materials in the row B are divided into two paths through the material distributing valve (5), wherein one path enters the decomposing furnace (3) and the other path enters the smoke chamber (6). The fuel enters the decomposing furnace (3) through a fuel inlet (4) of the decomposing furnace, the fuel in the decomposing furnace (3) is combusted to release a large amount of heat for decomposing the raw meal, the decomposed hot raw meal leaves the decomposing furnace (3) and enters the rotary kiln (7) after gas-solid separation by the lowest cyclone separator in the column A, the hot raw meal is calcined in the rotary kiln (7) to form clinker, the clinker enters the cooling machine (10) from the outlet of the rotary kiln (7), and then the clinker is cooled to 65 ℃ plus ambient temperature by the cooling machine (10); flue gas generated by fuel combustion and raw material decomposition in the decomposing furnace (3) enters the bottom cyclone separator in the row A from the outlet of the decomposing furnace (3), is subjected to gas-solid separation with hot raw materials and then enters the bottom cyclone separator in the row A, the raw materials in the row A are preheated for multiple times in the cyclone separator and the connecting air pipe, and finally leaves from the outlet of the top cyclone separator in the row A.
The temperature of the flue gas discharged from a flue gas outlet (15) of the A-row cyclone preheater is 300-400 ℃, and CO in the flue gas2The concentration is more than 70 percent, and CO with purity of more than 99 percent can be obtained by the processes of purification, drying, trapping, purification and the like2Then carrying out resource treatment or sealing. The air at the ambient temperature cools the high-temperature clinker entering from the outlet of the rotary kiln (7) through a cooler (10), and the air after heat exchange is divided into three paths: the first path of air enters the rotary kiln (7) to be used as high-temperature secondary air (900-1200 ℃) for fuel combustion. The second path of high-temperature air (800-1000 ℃) enters a tertiary air pipe (8) as tertiary air, oxygen enters a heat exchanger (14) through a gas inlet (1401), the tertiary air preheats the oxygen through the heat exchanger (14), the preheated oxygen enters a decomposing furnace (3) through a pipeline, total oxygen is combusted in the decomposing furnace (3), and the preheated tertiary air enters a waste heat utilization or treatment system. And the third path of air (250-450 ℃) enters a waste heat boiler for power generation or other waste heat utilization or treatment systems, and the air of the power generation or other waste heat utilization or treatment systems is discharged into the atmosphere through a chimney after passing through a waste air treatment system.
Kiln gas formed by fuel combustion and little raw material decomposition in the rotary kiln (7) is subjected to gas-solid separation with raw material in the row B through the lowest stage cyclone separator in the row B, the separated flue gas is subjected to multiple preheating on the raw material in the row B through the cyclone preheater in the row B, and finally the flue gas leaves from a flue gas outlet (16) of the cyclone preheater in the row B; the temperature of flue gas at the outlet of the B-row cyclone preheater is 300-400 ℃, and CO in the flue gas2The concentration is about 25 percent, then the flue gas enters a waste heat boiler for power generation or other waste heat utilization or treatment systems, and the flue gas after power generation or other waste heat utilization and treatment systems passes through a waste air treatment system and then passes through a chimneyAnd is vented to the atmosphere.
In the second case: valve A (13) is fully closed, valve B (11) and valve C (12) are fully opened, and the cement predecomposition kiln is used as CO2Self-enrichment type pre-decomposition kiln.
The difference from the first case is that: a part of smoke discharged from a smoke outlet (15) of the A-column cyclone preheater is used as circulating smoke, mixed gas of the circulating smoke and oxygen is conveyed into a heat exchanger (14) through a gas inlet (1401), tertiary air and the mixed gas perform heat exchange in the heat exchanger (14), the mixed gas after the heat exchange is conveyed into a decomposing furnace (3) through a pipeline, and oxygen-enriched combustion is performed in the decomposing furnace (3).
In the third case: the valve A (13) is fully opened, the valve B (11) and the valve C (12) are fully closed, and the cement predecomposition kiln is used as a linear separation predecomposition kiln.
In this case, the flow direction of the material in the system is the same as in the first and second cases, and the flow direction of the gas is different from the first and second cases.
The air at the ambient temperature cools the high-temperature clinker entering from the outlet of the rotary kiln (7) through a cooler (10), and the air after heat exchange is divided into three paths: the first path of air enters the rotary kiln (7) as high-temperature secondary air (900-1200 ℃) for fuel combustion, the second path of air enters the tertiary air pipe (8) as tertiary air (800-1000 ℃) and the tertiary air directly enters the decomposing furnace (3) for fuel combustion. And (3) allowing the third path of air (250-450 ℃) to enter a waste heat boiler for power generation or other waste heat utilization or treatment systems, and exhausting the air of the power generation or other waste heat utilization or treatment systems into the atmosphere through a chimney after the air passes through a waste air treatment system.
Kiln gas formed by fuel combustion and little raw material decomposition in the rotary kiln (7) is subjected to gas-solid separation with the raw material in the column B through the lowest-stage cyclone separator in the column B, separated flue gas is subjected to multiple preheating on the raw material in the column B through the cyclone preheater in the column B, and finally the flue gas leaves from a flue gas outlet (16) of the cyclone preheater in the column B.
The flue gas formed in the decomposing furnace is discharged from a flue gas outlet (15) of the cyclone preheater in the row A through the cyclone preheater in the row A, and the flue gas formed in the rotary kiln is discharged from a flue gas outlet (16) of the cyclone preheater in the row B through the cyclone preheater in the row B) And (4) discharging. The temperature of flue gas discharged from a flue gas outlet (15) of the cyclone preheater in the row A and a flue gas outlet (16) of the cyclone preheater in the row B is 300-400 ℃, and CO in the flue gas discharged from the flue gas outlet (15) of the cyclone preheater in the row A is in the range of CO2The concentration is about 35 percent, and CO in the flue gas discharged from a flue gas outlet (16) of the B-row cyclone preheater2The concentration is about 25%. And then the flue gas enters a waste heat boiler for power generation or other waste heat utilization or treatment systems, and the flue gas after power generation or other waste heat utilization or treatment systems passes through a waste air treatment system and then is discharged into the atmosphere through a chimney.
In a fourth case: the valve A (13), the valve B (11) and the valve C (12) are all closed, the material distributing valve (5) distributes all preheated hot raw materials into the smoke chamber (6), and the cement precalcining kiln system is used as a preheater kiln.
Raw materials are not fed into the cyclone preheater in the column A, and no flue gas exists in the column A; raw materials are fed through a raw material feeding port (2) of the cyclone preheater B, the raw materials exchange heat with flue gas for multiple times through a cyclone separator and a connecting air pipe, and finally the raw materials can be preheated to 700-800 ℃; the preheated hot raw meal is distributed into the smoke chamber (6) through the distributing valve (5) and then conveyed to the rotary kiln (7). The hot raw meal is calcined in the rotary kiln (7) to form clinker, which enters the cooler (10) from the outlet of the rotary kiln (7) and is then cooled to 65 ℃ plus ambient temperature by the cooler (10).
The air under the environment temperature cools the high-temperature clinker falling from the outlet of the rotary kiln through a cooler (10), and the air after heat exchange is divided into two paths: the first path of air enters the rotary kiln and is used as high-temperature secondary air (900-1200 ℃) for fuel combustion. The second path of air (250-1000 ℃) enters a waste heat boiler for power generation or other waste heat utilization or treatment systems, and the air of the power generation or other waste heat utilization or treatment systems is discharged into the atmosphere through a chimney after passing through a waste air treatment system; kiln gas formed by combustion of fuel and decomposition of a small amount of raw materials in the rotary kiln (7) is subjected to gas-solid separation with the raw materials in the row B through the lowest-stage cyclone separator in the row B, separated flue gas is subjected to multiple preheating on the raw materials in the row B through the cyclone preheater in the row B, and finally the flue gas leaves from a flue gas outlet (16) of the cyclone preheater in the row B; the temperature of flue gas discharged from a flue gas outlet (16) of the B-row cyclone preheater is 300-400 ℃, and CO in the flue gas2The concentration is about 30%, then the flue gas enters a waste heat boiler for power generation or other waste heat utilization or treatment systems, and the flue gas after power generation or other waste heat utilization or treatment systems passes through a waste air treatment system and then is discharged into the atmosphere through a chimney.
The above description is only a preferred embodiment of the present invention and should not be taken as limiting, and any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention, such as adjusting the number of the cyclone preheater stages in the rows A and B, the mixing ratio of O2 and the circulating flue gas, the location of the raw material in the row B into the rotary kiln, etc., should be included in the protection scope of the present invention.
Claims (13)
1. A cement predecomposition kiln system which is characterized in that,
the system comprises a first row of cyclone preheaters, a second row of cyclone preheaters, a decomposing furnace, a smoke chamber, a rotary kiln, a cooler and a heat exchanger;
an air inlet of the first row of cyclone preheaters is connected with the decomposing furnace, and a discharge port of the first row of cyclone preheaters is connected with the smoke chamber; the air inlet of the second row of cyclone preheaters is connected with the smoke chamber, the discharge port of the second row of cyclone preheaters is divided into two paths, one path is connected with the decomposing furnace, and the other path is connected with the smoke chamber;
the smoke chamber is connected with the rotary kiln; the rotary kiln is connected with a cooler;
the cooler is provided with a tertiary air pipe, the tertiary air pipe is divided into two paths through a switching part, one path is that the tertiary air pipe is connected with a heat exchanger, and the heat exchanger is connected with the decomposing furnace through a pipeline; the other path is that the tertiary air pipe is directly connected with the decomposing furnace without a heat exchanger;
the switching component is selected from a valve;
the valves comprise 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 on a pipeline connecting the heat exchanger and the decomposing furnace;
the first valve is arranged on a tertiary air pipe connecting the cooler and the heat exchanger, and the second valve is arranged on a pipeline connecting the heat exchanger and the decomposing furnace; the third valve is arranged on a tertiary air pipe which connects the cooler and the decomposing furnace;
when the third valve is closed and the first valve and the second valve are opened, the tertiary air heats the mixed gas or oxygen of the circulating flue gas and the oxygen through the heat exchanger, the mixed gas or oxygen of the circulating flue gas and the oxygen enters the decomposing furnace, the oxygen-enriched combustion or the total oxygen combustion is carried out in the decomposing furnace, and the CO is adopted as the system at the moment2A self-enrichment type pre-decomposition kiln;
when the third valve is opened and the first valve and the second valve are closed, the tertiary air pipe is directly connected with the decomposing furnace, hot air in the tertiary air pipe enters the decomposing furnace, and the system is an off-line type pre-decomposing kiln at the moment;
when the first valve, the second valve and the third valve are all closed, the first row of cyclone preheaters do not feed raw materials any more, the fuel in the decomposing furnace is not supplied any more, when the material distributing valve distributes all the hot raw materials preheated in the second row of cyclone preheaters into the smoke chamber, the hot raw materials enter the rotary kiln and are calcined in the rotary kiln to form clinker, the clinker enters a cooler from the outlet of the rotary kiln and is then cooled by the cooler to obtain cement clinker, and at the moment, the system is a preheater kiln.
2. The cement precalciner system according to claim 1, wherein a distributing valve is arranged at the discharge port of the second row of cyclone preheater, one end of the distributing valve is connected with the decomposing furnace, and the other end of the distributing valve is connected with the smoke chamber.
3. The cement precalciner system according to claim 1 or 2, wherein the distributing valve distributes the raw meal passing through the outlet of the second row of cyclone preheater to the decomposing furnace, the smoke chamber; the feed divider adjusts the raw material amount entering the decomposing furnace and the smoke chamber from the discharge port of the second row of cyclone preheaters.
4. The cement precalciner system of claim 1, wherein the valve is selected from a gate valve or a butterfly valve.
5. The cement precalciner system of claim 1 wherein the first and second series of cyclone preheaters have a number of stages selected from 3 to 7.
6. The cement precalciner system of claim 1 wherein the heat exchanger has one or more gas inlets, one or more gas outlets;
one of the gas outlets is connected with a waste heat utilization or treatment system; the waste heat utilization or treatment system comprises a waste heat boiler for generating electricity and drying materials;
the cooler is selected from one of a grate cooler, a single-cylinder cooler and a multi-cylinder cooler.
7. A method of preparing cement clinker using the cement precalciner system of any of claims 1 to 6, characterized in that the method comprises:
respectively adding the raw materials into a first row of cyclone preheaters and a second row of cyclone preheaters, and exchanging heat between the raw materials and the flue gas in the cyclone preheaters;
the raw materials preheated by the first row of cyclone preheaters enter the decomposing furnace through one point or multiple points, the raw materials preheated by the second row of cyclone preheaters can be divided into two paths, wherein one path enters the decomposing furnace through one point or multiple points, and the other path enters the rotary kiln through the smoke chamber;
the hot raw materials decomposed in the decomposing furnace leave the decomposing furnace and enter a last-stage cyclone separator of a first row of cyclone preheaters, the hot raw materials enter a rotary kiln through a smoke chamber after gas-solid separation, the raw materials are calcined in the rotary kiln to form clinker, the clinker enters a cooler from an outlet of the rotary kiln and is cooled by the cooler, and cement clinker is obtained;
kiln gas formed in the rotary kiln is subjected to gas-solid heat exchange by the second row of cyclone preheaters and then is discharged from the outlet of the uppermost stage of cyclone separator; the flue gas formed in the decomposing furnace is subjected to gas-solid heat exchange by the first row of cyclone preheaters and then is discharged from the outlet of the uppermost stage of cyclone separator;
the tertiary air is divided into two paths by the switching component, and any one of the following paths is selected by adjusting the switching component: one path is that the tertiary air enters a heat exchanger through a tertiary air pipe, the tertiary air and the mixed gas of oxygen and circulating flue gas or the oxygen carry out heat exchange through the heat exchanger, the mixed gas of the circulating flue gas and the oxygen or the oxygen which are subjected to the heat exchange enter a decomposing furnace, the tertiary air which is subjected to the heat exchange enters a waste heat utilization or treatment system, the other path is that the tertiary air directly enters the decomposing furnace through the tertiary air pipe without passing through the heat exchanger, and the hot air in the tertiary air pipe enters the decomposing furnace.
8. Method for manufacturing cement clinker according to claim 7, wherein the raw meal is fed through the inlet duct of the uppermost cyclone of the first and second series of cyclone preheaters or through the inlet duct of the uppermost second cyclone of the first and second series of cyclone preheaters.
9. The method for manufacturing cement clinker according to claim 7, wherein when the switching unit is switched to the tertiary air duct connected to the heat exchanger connected to the decomposing furnace through the duct, the mixed gas of the circulating flue gas and the oxygen or the oxygen exchanges heat with the hot air in the tertiary air duct through the heat exchanger, the tertiary air after heat exchange enters the waste heat utilization or treatment system, the mixed gas of the circulating flue gas and the oxygen or the oxygen after heat exchange enters the decomposing furnace, and the decomposing furnace is either oxycombustion or oxy-fuel combustion.
10. The method for manufacturing cement clinker according to claim 7, wherein when the third valve is closed and the first valve and the second valve are opened, the tertiary air passes through the heat exchanger to heat oxygen and enters the decomposing furnace, and the decomposing furnace is in oxy-fuel combustion;
when the third valve is closed and the first valve and the second valve are opened, the tertiary air heats the mixed gas of the circulating flue gas and the oxygen through the heat exchanger and enters the decomposing furnace, and the oxygen-enriched combustion is performed in the decomposing furnace.
11. Method for manufacturing cement clinker according to any of claims 7 to 10, wherein, in the gas flow direction,the air cools the high-temperature clinker through a cooler, and the air after heat exchange is divided into the following three paths: the first path of high-temperature air is used as secondary air and directly enters the rotary kiln for fuel combustion; when the third valve is fully closed and the first valve and the second valve are fully opened, the system is used as CO2When the self-enrichment type pre-decomposition kiln is used, the second path of high-temperature air is used as tertiary air to preheat the mixed gas of the circulating flue gas and the oxygen or the oxygen through a heat exchanger, the preheated tertiary air enters a waste heat utilization or treatment system, and the preheated mixed gas of the circulating flue gas and the oxygen or the oxygen enters a decomposition furnace; when the third valve is fully opened and the first valve and the second valve are fully closed, namely the system is used as an offline pre-decomposition kiln, the second path of high-temperature air is used as tertiary air to directly enter the decomposition furnace for fuel combustion, and oxygen or mixed gas of the oxygen and circulating flue gas is not supplied into the decomposition furnace; and the third path of air enters a waste heat utilization or treatment system.
12. The method for manufacturing cement clinker according to claim 11, wherein the air outlet of the cooler is a first path, a second path, and a third path; or the first path independently exhausts air, and the second path and the third path are combined to exhaust air.
13. The method for preparing cement clinker according to claim 12, wherein the combined outlet air of the second path and the third path is an outlet air pipe shared by the second path and the third path;
when the first valve, the second valve and the third valve are all closed, the first row of cyclone preheaters do not feed raw materials, the fuel in the decomposing furnace is not supplied any more, and when the material distributing valve distributes all the hot raw materials preheated in the second row of cyclone preheaters into the smoke chamber, namely when the system is used as a preheater kiln, the first path independently exhausts air, and the second path and the third path are combined to exhaust air.
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| PCT/CN2019/100164 WO2021026714A1 (en) | 2019-08-12 | 2019-08-12 | Cement pre-calciner kiln system and method for preparing cement clinker |
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| CN113606946B (en) * | 2021-07-23 | 2023-04-28 | 中国中材国际工程股份有限公司 | Carbon dioxide capturing system and emission reduction method for cement kiln tail flue gas |
| CN114163151B (en) * | 2021-11-23 | 2022-11-08 | 天津水泥工业设计研究院有限公司 | By using CO 2 Carbon emission reduction method and system for storing solar energy to calcine cement clinker |
| CN114907033B (en) * | 2022-07-01 | 2023-04-14 | 天津水泥工业设计研究院有限公司 | Production of cement clinker and CO-production of liquid CO by oxy-fuel combustion 2 System and method |
| CN116105492B (en) * | 2023-04-12 | 2023-06-16 | 中材建设有限公司 | Carbon capture auxiliary system for cement production line and CO2 sealing method |
| CN116535117A (en) * | 2023-05-08 | 2023-08-04 | 天津水泥工业设计研究院有限公司 | Metakaolin preparation system and method capable of realizing decoupling function |
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