CN112654590B - Cement kiln system capable of adjusting CO2 enrichment amount and improved by online decomposing furnace and using method thereof - Google Patents
Cement kiln system capable of adjusting CO2 enrichment amount and improved by online decomposing furnace and using method thereof Download PDFInfo
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- CN112654590B CN112654590B CN201980054910.9A CN201980054910A CN112654590B CN 112654590 B CN112654590 B CN 112654590B CN 201980054910 A CN201980054910 A CN 201980054910A CN 112654590 B CN112654590 B CN 112654590B
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
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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
- F27B17/00—Furnaces of a kind not covered by any preceding group
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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
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Abstract
The invention relates to an adjustable CO modified by an online decomposing furnace2An enrichment cement kiln system and method. By means of the regulating function of the components of the invention, the system can be switched to CO2Self-enriching type pre-decomposition kiln or conventional on-line type pre-decomposition kiln. The invention can be based on CO2The required quantity of the system, and further flexibly adjusting the CO of the cement kiln system2And (4) enriching amount. Moreover, the cement kiln system of the present invention allows for CO production without redesigning critical firing equipment2Enrichment and reduction of reconstruction cost. Furthermore, when the system of the present invention is used as a CO2In the self-enrichment type pre-decomposition kiln, CO in the flue gas at the outlet of the third row of cyclone preheaters2The concentration is more than 70 percent, and the subsequent CO can be greatly reduced2High CO capture, purification and operation cost2The concentration flue gas amount can be flexibly adjusted to 5-30% of the outlet flue gas amount of the preheater of the conventional predecomposition kiln system, so that the CO content of the predecomposition kiln system is greatly reduced2And (4) discharging the amount.
Description
Technical Field
The invention belongs to the technical field of carbon emission reduction in cement industry, and particularly relates to an adjustable CO reformed by an online decomposing furnace2An enrichment cement kiln system and method.
Background
CO, a major greenhouse gas2The global greenhouse effect is aggravated by a large amount of emission, and countries in the world generally face the difficult tasks 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 become the second largest CO after the electricity industry2A source of emissions. According to statistics, the yield of the Chinese cement clinker in 2018 is close to 19 hundred million tons, and CO is generated in the prior art for producing 1 ton of cement clinker2CO emission of about 0.84 tons2Emissions 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. Research on carbon emission reduction technologies has been reported at home and abroad, but the research is mainly oriented to industries such as electric power, coal, steel and the like, and relatively few reports on carbon emission reduction technologies related to the cement industry are reported. The cement production process adopts a novel dry production process, and mainly comprises a cooler, a combustor, a rotary kiln, a multistage cyclone preheater, a connecting air pipe and the like. The raw meal is preheated in a cyclone preheater and is decomposed in a decomposing furnace, part of fuel is combusted in the decomposing furnace to provide heat required by the decomposition of the raw meal, the decomposed raw meal is calcined into cement clinker by the other part of fuel in a rotary kiln, and then the cement clinker is cooled to a proper temperature by a cooler. The gas introduced into the cement kiln system is air, and the outlet CO of the preheater2The concentration is about 30%. The current carbon emission reduction technical scheme adopted by the cement industry is pre-combustion capture and post-combustion capture. Wherein the pre-combustion capture refers to pretreatment of the fuel before combustion to separate carbon from the fuel. Due to the characteristics of cement clinker production process, CO before combustion2One significant disadvantage of capture is that only the CO produced by combustion of the fuel can be separated2And about 60% of CO generated 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 calcining process has very harsh conditions for hydrogen combustion, and a rotary kiln combustor needs to be specially designed, so 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 all have the problems of low carbon capture efficiency, small capture flow, complex system, large equipment investment or higher operation cost.
Disclosure of Invention
In view of the above problems, the present invention provides an adjustable CO reformed by an in-line type decomposing furnace2An enrichment cement kiln system, the cement kiln system comprising: the device comprises a first row of cyclone preheaters, a second row of cyclone preheaters, a third row of cyclone preheaters, a first decomposing furnace, a second decomposing furnace, a smoke chamber, a rotary kiln and a cooler;
the air inlets of the first row of cyclone preheaters and the second row of cyclone preheaters are connected with the first decomposing furnace; the discharge port of the first row of cyclone preheaters or the discharge port of the second row of cyclone preheaters is connected with the second decomposing furnace; the air inlet of the third row of cyclone preheaters is connected with the second decomposing furnace, and the discharge hole of the first-to-last cyclone separator of the third row of cyclone preheaters is connected with the smoke chamber;
the first decomposing furnace is connected with a smoke chamber, and the smoke chamber is connected with the rotary kiln; the rotary kiln is connected with a cooler.
According to the invention, the fraction of the hot raw meal preheated to completion by the first or second series of cyclone preheaters or both can be distributed to the second decomposing furnace.
According to the embodiment of the invention, a first material distributing valve is arranged at a discharging pipe of the penultimate cyclone separator of the second row of cyclone preheaters, one end of the first material distributing valve is connected with the first decomposing furnace, and the other end of the first material distributing valve is connected with the second decomposing furnace.
According to an embodiment of the invention, the penultimate cyclone of the first train of cyclone preheaters is connected to the first decomposing furnace by a duct, which does not contain a bypass or contains a bypass;
when the pipeline does not comprise a branch, the first row of cyclone preheaters feeds the first decomposing furnace at a single point;
when the pipeline comprises a branch, the first row of cyclone preheaters feeds the first decomposing furnace at multiple points; the pipeline comprises a conveying main road and conveying branch roads, the number of the conveying branch roads is more than 2, the conveying branch roads are connected in parallel, and a second distributing valve is arranged at the joint of the conveying main road and the conveying branch roads; the second material distributing valve is used for adjusting the material quantity entering the conveying branch from the conveying main path.
According to the embodiment of the invention, the number of the stages of the first row of cyclone preheaters and the number of the stages of the second row of cyclone preheaters are selected from 3-7 stages;
the third row of cyclone preheaters has the number of stages selected from 1-5.
According to the embodiment of the invention, the cooler is selected from one of a grate cooler, a single-cylinder cooler and a multi-cylinder cooler;
the cement kiln system also comprises a tertiary air pipe; one end of the tertiary air pipe is connected with the cooling machine, and the other end of the tertiary air pipe is connected with the first decomposing furnace.
According to the embodiment of the invention, the cement kiln system further comprises a cooler, and the air outlet of the third row of cyclone preheaters is connected with the cooler; and the cooler is used for cooling the flue gas discharged from the air outlet of the third row of cyclone preheaters.
According to the embodiment of the invention, the first row of cyclone preheaters and the second row of cyclone preheaters are provided with feeding ports, and the feeding ports are arranged at inlet air pipes of uppermost first-stage cyclone separators of the first row of cyclone preheaters and the second row of cyclone preheaters or at inlet air pipes of uppermost second-stage cyclone separators of the first row of cyclone preheaters and the second row of cyclone preheaters;
a feed inlet is arranged or not arranged on the third row of cyclone preheaters;
when the stage number of the third row of cyclone preheaters is 1 grade, the air outlet of the third row of cyclone preheaters is connected with the cooler, and at the moment, no feeding hole is arranged on the third row of cyclone preheaters;
when the stage number of the third row of cyclone preheaters is more than 2, a feeding hole is formed in the third row of cyclone preheaters;
specifically, when the number of the third row of the cyclone preheaters is 2, the feed inlet of the third row of the cyclone preheaters is arranged at the inlet air pipe of the uppermost first-stage cyclone separator of the third row of the cyclone preheaters;
when the number of the third row of the cyclone preheaters is more than 3, the feed inlet of the third row of the cyclone preheaters is arranged at the inlet air pipe of the uppermost first-stage cyclone separator of the third row of the cyclone preheaters or at the inlet air pipe of the uppermost second-stage cyclone separator of the third row of the cyclone preheaters.
According to the embodiment of the invention, when the third row of cyclone preheaters has more than 2 stages, a communicating pipeline is arranged between the third row of cyclone preheaters and the first row of cyclone preheaters, and/or a communicating pipeline is arranged between the third row of cyclone preheaters and the second row of cyclone preheaters; the communicating pipeline is used for conveying the raw meal preheated by the third row of cyclone preheaters to the first row of cyclone preheaters or the second row of cyclone preheaters or simultaneously conveying the raw meal to the first row of cyclone preheaters and the second row of cyclone preheaters;
one end of the communicating pipeline is arranged at a discharge port of a last but one second cyclone separator of the third row of cyclone preheaters;
the other end of the communicating pipeline is arranged on an inlet air pipe of a first-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater, or on an inlet air pipe of a second-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater, or on an inlet air pipe of a third-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater, or on an inlet air pipe of a fourth-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater, or on an inlet air pipe of a fifth-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater.
According to the embodiment of the invention, the cement kiln system further comprises a heat exchanger, the tertiary air pipe is divided into two paths, one end of the tertiary air pipe is connected with the cooling machine, and the other end of the tertiary air pipe is connected with the first decomposing furnace; the other path is a tertiary air pipe, the other end of the tertiary air pipe is connected with a heat exchanger, and the heat exchanger is connected with a second decomposing furnace through a pipeline.
For example, the tertiary air duct can be divided into two paths by arranging two pipelines, or a main path and a branch path are arranged on the tertiary air duct.
Specifically, when two pipelines are arranged, one ends of the two pipelines are connected with the cooler; the other end of the first pipeline is connected with the first decomposing furnace, the other end of the second pipeline is connected with the heat exchanger, and the heat exchanger is connected with the second decomposing furnace through a pipeline;
when the main path and the branch path are arranged on the tertiary air pipe, one end of the main path is connected with the cooling machine, and the other end of the main path is connected with the first decomposing furnace; one end of the branch is connected with the main road, the other end of the branch is connected with the heat exchanger, and the heat exchanger is connected with the second decomposing furnace through a pipeline.
The invention also provides an adjustable CO modified by the online decomposing furnace by using the adjustable CO2A method for producing cement clinker in an enriched cement kiln system, the method comprising:
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 meal preheated by the first row of cyclone preheaters and the second row of cyclone preheaters enters the first decomposing furnace through one or more points; part of the hot raw meal preheated by the first row of cyclone preheaters or the second row of cyclone preheaters or the first row and the second row of cyclone preheaters enters the second decomposing furnace through one or more points;
the decomposed hot raw materials leave the first decomposing furnace and the second decomposing furnace, are separated from the flue gas and then enter the rotary kiln, are calcined in the rotary kiln to form cement clinker, and the clinker enters a cooler from the outlet of the rotary kiln;
the mixed gas of oxygen and circulating flue gas or oxygen is conveyed into a second decomposition furnace, the second decomposition furnace is oxygen-enriched combustion or total oxygen combustion, and high CO generated in the second decomposition furnace2The concentrated flue gas is discharged through a third row of cyclone preheaters; the CO can be regulated by regulating the amount of hot raw meal entering the second decomposition furnace2And (4) enriching amount.
According to the invention, the raw meal may or may not be fed to the third row of cyclone preheaters.
According to the embodiment of the invention, the raw meal preheated by the second row of cyclone preheaters is divided into two paths by the first material dividing valve, wherein one path enters the first decomposing furnace, and the other path enters the second decomposing furnace.
According to the embodiment of the invention, raw meal is respectively fed into a first row of cyclone preheaters and a second row of cyclone preheaters, the raw meal preheated by the first row of cyclone preheaters and the second row of cyclone preheaters enters a first decomposing furnace, the amount of hot raw meal is conveyed into a second decomposing furnace through regulating of a first material distributing valve, and oxygen-enriched combustion or total oxygen combustion is carried out in the second decomposing furnace, wherein the system is CO2The self-enrichment type pre-decomposition kiln can adjust the amount of the hot raw materials entering the second decomposition furnace through adjusting the first material distributing valve2Enriching amount;
raw materials are respectively fed into a first row of cyclone preheaters and a second row of cyclone preheaters, the raw materials preheated by the first row of cyclone preheaters and the second row of cyclone preheaters enter a first decomposing furnace, a first material distributing valve is adjusted to enable all the raw materials preheated by the second row of cyclone preheaters to be conveyed to the first decomposing furnace, the second decomposing furnace, the third row of cyclone preheaters and a cooler are stopped to be used, and at the moment, the system is a conventional online type pre-decomposing kiln.
According to an embodiment of the invention, when raw meal is fed to the third row of cyclone preheaters, the preheated raw meal from the third row of cyclone preheaters is fed via the connecting duct to the first row of cyclone preheaters or to the second row of cyclone preheaters, or to both the first row of cyclone preheaters and the second row of cyclone preheaters.
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 comprises 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; the second path of high-temperature air is used as tertiary air and directly enters the first decomposing furnace for fuel combustion; and the third path of air with higher temperature enters a waste heat boiler for power generation or other waste heat utilization or treatment systems, and the flue gas after power generation is completed or other waste heat utilization or treatment systems is treated by the waste air and then is discharged into the atmosphere through a chimney.
According to the embodiment of the invention, the second path of high-temperature air is divided into two paths as tertiary air, wherein one path of tertiary air enters the first decomposing furnace through the tertiary air pipe; the other path of tertiary air enters a heat exchanger through a tertiary air pipe, the mixed gas of oxygen and circulating flue gas or oxygen enters the heat exchanger, the mixed gas of oxygen and circulating flue gas or oxygen after heat exchange enters a second decomposition furnace through a pipeline, and oxygen-enriched combustion or total oxygen combustion is carried out in the second decomposition furnace; the tertiary air after heat exchange enters a waste heat utilization or treatment system;
the waste heat utilization or treatment system comprises waste heat power generation and material drying.
Compared with the prior art, the invention has the following advantages and effects:
1. by means of the regulating function of the components of the invention, the system can be switched to CO2Self-enriching type pre-decomposition kiln or conventional on-line type pre-decomposition kiln. Although carbon emission reduction is largely implemented in the cement industry, at present, China is dealing with food-grade or industrial-grade CO2The market demand of the product is limited. Taking a 5500t/d scale cement clinker production line as an example, if CO in kiln tail flue gas is treated2All collected and purified into food grade or industrial grade CO2The product is enough to satisfy most of the CO in China2The requirement of (2) is to point out that the total number of the cement clinker production lines of different scales in China currently exceeds 1000. Based on the above considerations, it can be based on CO2The demand of the product adjusts the components of the system of the invention, thereby flexibly adjusting the CO of the cement kiln system2Enrichment ofAnd (4) realizing carbon emission reduction in the cement industry. When it is against CO2When the demand of the product is not high, CO can not be carried out in the cement kiln2Self-enrichment does not affect the normal production of cement clinker;
2. the cement kiln system can carry out CO sintering without redesigning key sintering equipment such as a rotary kiln, a cooler and the like2Enrichment, greatly simplifying the process flow, reducing the modification cost, and being suitable for modifying most of the existing pre-decomposition kiln systems or designing newly-built pre-decomposition kiln systems;
3. the conventional precalciner kiln system has large outlet flue gas amount and CO2The concentration is about 30 percent, and the CO content in the flue gas is adjusted2The investment cost and the operation cost of the trapping and purifying system are high when the trapping and purifying are carried out to the food-grade or industrial-grade concentration. When the system of the invention is used as CO2When the self-enrichment type pre-decomposition kiln is used, CO in flue gas at the outlets of the first row of cyclone preheaters and the second row of cyclone preheaters2The concentration is about 30 percent, and CO is contained in the flue gas at the outlet of the third row of cyclone preheaters2The concentration is more than 70 percent, and the subsequent CO can be greatly reduced2Investment cost and operation cost of the capture and purification system, and high CO2The concentration flue gas amount can be flexibly adjusted to 5-30% of the outlet flue gas amount of the preheater of the conventional predecomposition kiln system, so that the CO content of the predecomposition kiln system is greatly reduced2And (4) discharging the amount.
Drawings
FIG. 1 is a schematic view showing an adjustable CO reformed by an in-line type decomposing furnace in example 1 of the present invention2Cement kiln map of enrichment amount;
FIG. 2 is a schematic view showing an adjustable CO reformed by an in-line type decomposing furnace in example 2 of the present invention2Cement kiln map of enrichment amount;
FIG. 3 is a partial schematic view of a tertiary air duct in example 3;
wherein, the feeding hole of the cyclone preheater of 1-A row, the feeding hole of the cyclone preheater of 2-B row, the feeding hole of the cyclone preheater of 3-C row, the burner of 4-decomposing furnace, the burner of 5-decomposing furnace A, 6-second material separating valve, 7-first material separating valve, the air inlet of 8-decomposing furnace B, 9-decomposing furnace B, 10-tertiary air pipe, the burner of 11-rotary kiln, 12-cooler, 13-blower, 14-rotary kiln, 15-smoke chamber, the smoke outlet of 16-A row, the smoke outlet of 17-B row, the smoke outlet of 18-C row, the smoke outlet of 19-cooler, the smoke outlet of 20-cooler, 21-heat exchanger, 2101-gas inlet, 2102-gas outlet.
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 do not 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.
Example 1
As shown in FIG. 1, CO can be adjusted2The cement kiln system for enriching the cement comprises a cyclone preheater A, a cyclone preheater B, a cyclone preheater C, a decomposing furnace A (5), a decomposing furnace B (8), a smoke chamber (15), a rotary kiln (14) and a cooler (12); air inlets of the cyclone preheaters of the A row and the B row are connected with a decomposing furnace A (5), and discharge outlets of the last cyclone separators of the cyclone preheaters of the A row and the B row are connected with a smoke chamber (15); an air inlet of the cyclone preheater in the row C is connected with a decomposing furnace B (8), and a discharge port of the cyclone preheater in the row C is connected with a smoke chamber (15); the decomposing furnace A (5) is connected with a smoke chamber (15), and the smoke chamber (15) is connected with the rotary kiln (14); the rotary kiln (14) is connected with a cooler (12). The decomposing furnace A (5) and the decomposing furnace B (8) are both provided with a burner (4) of the decomposing furnace; a combustor (11) of the rotary kiln is arranged on the rotary kiln (14); a tertiary air pipe (10) is arranged on the cooling machine (12); a fan (13) is arranged below the cooler (12).
A first distributing valve (7) is arranged at a discharging pipe of a penultimate secondary cyclone separator of the B-row cyclone preheater, one end of the first distributing valve (7) is connected with the decomposing furnace A (5), and the other end of the first distributing valve (7) is connected with the decomposing furnace B (8).
The last-but-one secondary cyclone separator of the cyclone preheater in the row A is connected with the decomposing furnace A (5) through a pipeline, the pipeline comprises a branch, and the cyclone preheater in the row A feeds the decomposing furnace A (5) at multiple points; the pipeline comprises a conveying main road and conveying branch roads, the number of the conveying branch roads is more than 2, the conveying branch roads are connected in parallel, and a second distributing valve (6) is arranged at the joint of the conveying main road and the conveying branch roads; one end of the second distributing valve (6) is connected with the conveying main path, and other ports of the second distributing valve (6) are connected with the conveying branch path; the second material distributing valve (6) can adjust the material quantity entering the conveying branch from the conveying main path.
The cooler (12) is selected from one of a grate cooler, a single-cylinder cooler and a multi-cylinder cooler;
the cyclone preheater A, the cyclone preheater B and the cyclone preheater C are respectively provided with a feeding hole, and the feeding hole (1) of the cyclone preheater A, the feeding hole (2) of the cyclone preheater B and the feeding hole (3) of the cyclone preheater C are arranged at the inlet air pipes of the uppermost first-stage cyclone separators of the cyclone preheaters A, B and C. According to the requirement, the feeding hole can also be arranged at the inlet air pipes of the uppermost second-stage cyclone separators of the cyclone preheaters in the A column, the B column and the C column. Optionally, the cyclone preheater of column C may be provided with or without a feed inlet. Specifically, when the number of the C-column cyclone preheater stages is 2, the feed inlet of the C-column cyclone preheater is arranged at the inlet air pipe of the uppermost first-stage cyclone separator of the C-column cyclone preheater. When the number of the stages of the C-column cyclone preheater is more than 3, the feeding hole of the C-column cyclone preheater is arranged at the inlet air pipe of the uppermost first-stage cyclone separator of the C-column cyclone preheater or at the inlet air pipe of the uppermost second-stage cyclone separator of the C-column cyclone preheater.
And a communicating pipeline is arranged between the cyclone preheaters in the row C and the cyclone preheaters in the row B and is used for conveying the raw meal preheated by the cyclone preheaters in the row C to the cyclone preheaters in the row B. According to the requirement, a communicating pipeline can be arranged between the cyclone preheaters in the C row and the cyclone preheaters in the A row, and/or a communicating pipeline is arranged between the cyclone preheaters in the C row and the cyclone preheaters in the B row; the communicating pipeline is used for conveying the raw meal preheated by the cyclone preheater in the row C to the cyclone preheater in the row A or the cyclone preheater in the row B or simultaneously conveying the raw meal to the cyclone preheater in the row A and the cyclone preheater in the row B.
Through adjustment of the components, the system can be switched to CO2Self-enriching type pre-decomposition kiln or conventional on-line type pre-decomposition kiln. Specifically, the system can be switched to any one of the following three cases by adjustment of the components.
In the first case: raw meal is fed into the system through a feeding hole (1) of a row of cyclone preheaters, a feeding hole (2) of a row of cyclone preheaters and a feeding hole (3) of a row of cyclone preheaters, hot raw meal in the row of cyclone preheaters is distributed to a decomposing furnace A (5) and a decomposing furnace B (8) through a first material distributing valve (7), oxygen enters the decomposing furnace B (8) through an air inlet (9) of the decomposing furnace B, the inside of the decomposing furnace B (8) is in full-oxygen combustion, and the system is CO2Self-enrichment type pre-decomposition kiln.
Raw materials are respectively fed into the cyclone preheaters of the A row, the B row and the C row by a feeding device through a hoister, and preheating and gas-solid separation are realized in the cyclone preheaters. The raw material in the A row enters a decomposing furnace A (5) from a penultimate secondary cyclone separator in the A row after multiple heat exchange and gas-solid separation. The raw materials in the row B are divided into two paths in a first material dividing valve (7) after multiple heat exchange and gas-solid separation, wherein one path enters a decomposing furnace A (5), and the other path enters a decomposing furnace B (8).
The raw meal fed into the cyclone preheater of column C is used for cooling the high-temperature flue gas discharged from the decomposing furnace B (8). The raw meal preheated by the cyclone preheater in the row C enters the cyclone preheater in the row B through a communicating pipeline. One end of the communicating pipeline is arranged at a discharge hole of the last-but-one stage cyclone separator of the C-column cyclone preheater, and the other end of the communicating pipeline is arranged on an inlet air pipe of the uppermost first-stage cyclone separator of the B-column cyclone preheater. According to the requirement, the raw meal preheated in the C column can enter the cyclone preheater in the B column or the cyclone preheater in the A column or simultaneously enter the cyclone preheater in the A column and the cyclone preheater in the B column through the communicating pipeline, the feeding point of the communicating pipeline entering the cyclone preheater in the A column or the cyclone preheater in the B column can be arranged on an inlet air pipe of a first-stage cyclone separator at the top of the cyclone preheater in the A column or the cyclone preheater in the B column, or on an inlet air pipe of a second-stage cyclone separator at the top of the cyclone preheater in the A column or the cyclone preheater in the B column, or on an inlet air pipe of a fourth-stage cyclone separator at the top of the cyclone preheater in the A column or the cyclone preheater in the B column, or on an inlet air pipe of a fifth-stage cyclone separator at the top of the cyclone preheater in the A column or the cyclone preheater in the B column, the position of the specific feeding point can be adjusted according to the actual condition.
The fuel in the decomposing furnace is combusted to release a large amount of heat for decomposing the raw meal, the decomposed hot raw meal leaves the decomposing furnace A (5) and the decomposing furnace B (8), then enters the rotary kiln (14) after being separated from the flue gas, is calcined in the rotary kiln (14) to form clinker, and the clinker enters the cooler (12) from the outlet of the rotary kiln (14) and is then cooled to 65 ℃ plus the ambient temperature by the cooler (12).
It should be noted that, depending on the site arrangement of the pre-decomposition kiln system, it is also possible to consider the feeding of the partially preheated raw meal in column a to the decomposing furnace B (8) for endothermic decomposition, and in this case, it is possible to consider the feeding of the entire preheated raw meal in column B to the decomposing furnace a (5) for endothermic decomposition.
The air cools the high-temperature clinker through a cooler (12), and the air after heat exchange is mainly divided into the following three paths: the first path of high-temperature air (900-1200 ℃) is used as secondary air to directly enter the rotary kiln (14) for fuel combustion; a second path of high-temperature air (800-1000 ℃) is used as tertiary air and enters the decomposing furnace A (5) through a tertiary air pipe for fuel combustion; and the third path of air with higher temperature (250-450 ℃) can enter a waste heat boiler for power generation or other waste heat utilization or treatment systems, and the flue gas generated after power generation or other waste heat utilization or treatment systems is treated by waste air and then is discharged into the atmosphere through a chimney.
The pure oxygen obtained by the air separation device enters a decomposing furnace B (8) for burning the fuel entering the decomposing furnace B (8), and the decomposing furnace B(8) The inside is oxygen-rich combustion. Flue gas formed by combustion of fuel and decomposition of raw meal in the decomposing furnace B (8) leaves the decomposing furnace B (8) and enters the cyclone preheater in the row C, and then the raw meal in the row C is preheated, subjected to gas-solid separation and finally leaves from the outlet of the cyclone preheater in the row C. CO in flue gas exiting from a flue gas outlet (18) of the C-column cyclone preheater2The concentration is more than 70%, the flue gas temperature is controlled according to the number of cyclone separators arranged in the cyclone preheater in the row C, the raw material feeding amount in the cyclone preheater in the row C and the like, and the flue gas is dried and dedusted and CO is added2CO with the concentration of more than 99 percent and capable of being recycled can be obtained through a series of operations such as trapping, purification and the like2And (5) producing the product.
Kiln gas formed by combustion of fuel and decomposition of partial raw meal in the rotary kiln (14) enters a decomposing furnace A (5), flue gas formed by combustion of fuel and decomposition of raw meal in the decomposing furnace A (5) and kiln gas from the rotary kiln (14) leave the decomposing furnace A (5) and respectively enter a row A and a row B cyclone preheaters, then the row A and the row B raw meal are subjected to multiple preheating and gas-solid separation, and finally the flue gas respectively leaves from a flue gas outlet (16) of the row A cyclone preheater and a flue gas outlet (17) of the row B cyclone preheater. CO in flue gas discharged from outlets of cyclone preheaters in A and B rows2The concentration is about 30%, the temperature of the flue gas is 300-400 ℃, then the flue gas generates electricity through a kiln tail waste heat boiler, the raw material enters a raw material mill to dry the raw material, and then the flue gas is treated by a flue gas treatment system and then discharged into the atmosphere.
The amount of hot raw meal entering the decomposing furnace B (8) through adjusting the first material distributing valve (7) can adjust CO2And (4) enriching amount.
In the second case: the adjustment of each part of the system and the flow direction of materials and gas are the same as the first condition, the difference is that a part of the flue gas discharged from the outlet of the C-row cyclone preheater is used as circulating flue gas, the mixed gas of the circulating flue gas and oxygen enters a decomposing furnace B (8) through an air inlet (9) of the decomposing furnace B, the inside of the decomposing furnace B (8) is oxygen-enriched combustion, and the system is CO2Self-enrichment type pre-decomposition kiln.
CO in flue gas discharged from outlets of A-row cyclone preheater and B-row cyclone preheater2The concentration is about 30 percent, and CO in the flue gas discharged from the outlet of the C-row cyclone preheater2The concentration is more than 70 percent.
CO can be adjusted by adjusting the feeding amount of the first material distributing valve (7) into the decomposing furnace B (8)2And (4) enriching amount.
In the third case: raw materials are fed into the cyclone preheaters in the A row and the B row, raw materials are not fed into the cyclone preheater in the C row, and the raw materials in the A row and the raw materials in the B row are completely fed into the decomposing furnace A (5), the decomposing furnace B (8) and the cyclone preheater in the C row to be stopped, and the system is a conventional online type pre-decomposing kiln.
CO in flue gas discharged from outlets of the cyclone preheaters in the A row and the cyclone preheaters in the B row2The concentration is about 30%, and the flue gas temperature is 300-400 ℃.
Example 2
As shown in fig. 2, the connection relationship of the components of the system is the same as that of embodiment 1, except that the number of stages of the cyclone preheater in column C is 1, the air outlet of the cyclone preheater in column C is connected with a cooler (19), the cooler (19) is used for cooling the flue gas discharged from the cyclone preheater in column C, and the cooled flue gas is discharged from a flue gas outlet (20) of the cooler. By drying and dedusting the part of the flue gas and CO2CO with the concentration of more than 99 percent and capable of being recycled can be obtained through a series of operations such as trapping, purification and the like2And (5) producing the product.
The hot raw materials in the cyclone preheater B are conveyed to a decomposing furnace A (5) and a decomposing furnace B (8) through a first material distributing valve (7), the amount of the materials entering the decomposing furnace B (8) can be adjusted through the first material distributing valve (7), and then CO is adjusted2The enrichment amount of (a).
It should be noted that, depending on the site arrangement of the pre-decomposition kiln system, it is also possible to consider the feeding of the partially preheated raw meal in column a to the decomposing furnace B (8) for endothermic decomposition, and in this case, it is possible to consider the feeding of the entire preheated raw meal in column B to the decomposing furnace a (5) for endothermic decomposition.
Through adjustment of the components, the system can be switched to CO2Self-enriching type pre-decomposition kiln or conventional on-line type pre-decomposition kiln. Specifically, the system can be switched to any one of the following three cases by adjustment of the components.
In the first case: raw meal is fed into the system through a feed inlet (1) of the cyclone preheater in the row A and a feed inlet (2) of the cyclone preheater in the row BIn the system, hot raw meal in the cyclone preheater in the row B is distributed to a decomposing furnace A (5) and a decomposing furnace B (8) through a first material distributing valve (7), oxygen enters the decomposing furnace B (8) through an air inlet (9) of the decomposing furnace B, the decomposing furnace B (8) is internally combusted by total oxygen, and the system is CO2Self-enrichment type pre-decomposition kiln.
CO in flue gas discharged from outlets of the cyclone preheaters in the A row and the cyclone preheaters in the B row2The concentration is about 30 percent, and CO in the flue gas discharged from the outlet of the C-row cyclone preheater2Concentration of>70％。
Raw materials decomposed by the decomposing furnace B (8) enter a C-row cyclone separator connected with the decomposing furnace B (8) through a pipeline for gas-solid separation, the separated materials are conveyed into a smoke chamber (15) through a pipeline, the separated gas enters a cooler (19) through a pipeline for cooling, and CO in the cooled smoke gas2The concentration is more than 70 percent.
In the second case: the adjustment of each part of the system and the flow direction of materials and gas are the same as the first case, the difference is that a part of the flue gas discharged from the outlet of the cooler (19) is taken as the circulating flue gas, the mixed gas of the circulating flue gas and oxygen enters the decomposing furnace B (8) through the air inlet (9) of the decomposing furnace B, the inside of the decomposing furnace B (8) is oxygen-enriched combustion, and the system is CO2Self-enrichment type pre-decomposition kiln.
CO in flue gas discharged from outlets of A-row cyclone preheater and B-row cyclone preheater2The concentration is about 30 percent, and CO in the flue gas discharged from the outlet of the C-row cyclone preheater2At a concentration of>70％。
The CO can be adjusted by adjusting the feeding amount of the first material distributing valve (7) entering the decomposing furnace B (8)2And (4) enriching amount.
In the third case: raw materials are fed into the cyclone preheaters in the A row and the B row, raw materials are not fed into the cyclone preheater in the C row, the raw materials in the A row and the raw materials in the B row are all fed into the decomposing furnace A (5), the decomposing furnace B (8), the cyclone preheater in the C row and the cooler (19) are stopped to be used, and the system is a conventional online type pre-decomposing kiln.
CO in flue gas discharged from outlets of A-row cyclone preheater and B-row cyclone preheater2The concentration is about 30%.
Example 3
As shown in fig. 3, a tertiary air pipe (10) is arranged on the cooling machine (12), the tertiary air pipe (10) is divided into two paths, one end of the tertiary air pipe (10) is connected with the cooling machine (12), and the other end of the tertiary air pipe (10) is connected with the decomposing furnace a (5); the other path is a tertiary air pipe (10), the other end of the tertiary air pipe is connected with a heat exchanger (21), and the heat exchanger (21) is connected with a decomposing furnace B (8) through a pipeline.
The heat exchanger (21) is provided with a gas inlet (2101) and a gas outlet (2102). The gas outlet (2102) is connected with a waste heat utilization or treatment system, and the waste heat utilization or treatment system comprises waste heat power generation, material drying and the like. The mixed gas of the oxygen and the circulating flue gas or the oxygen is conveyed into the heat exchanger (21) through the gas inlet (2101), the tertiary air is conveyed into the heat exchanger (21) through the tertiary air pipe (10), and the mixed gas of the oxygen and the circulating flue gas or the oxygen and the tertiary air carry out heat exchange in the heat exchanger (21). The tertiary air after heat exchange enters a waste heat utilization or treatment system through a gas outlet (2102), and the mixed gas of oxygen and circulating flue gas after heat exchange or the oxygen enters a decomposing furnace B (8) through a pipeline.
When oxygen is conveyed to the heat exchanger (21), the tertiary air preheats the oxygen in the heat exchanger (21), the preheated oxygen enters the decomposing furnace B (8), and the decomposing furnace B (8) is in full-oxygen combustion.
When the mixed gas of the oxygen and the circulating flue gas is conveyed to the heat exchanger (21), the mixed gas of the oxygen and the circulating flue gas is preheated in the heat exchanger (21) by tertiary air, the preheated mixed gas of the oxygen and the circulating flue gas enters a decomposing furnace B (8), and oxygen-enriched combustion is performed in the decomposing furnace B (8).
The tertiary air pipe (10) and the heat exchanger (21) of example 3 can be applied to example 1 or example 2 or a known cement kiln system as required.
The above description is only a preferred embodiment of the present invention and should not be taken as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principles of the present invention, such as adjusting the number of the cyclone preheater stages in the row A, B or C, adjusting the position of the cyclone preheater in the row C to preheat the raw meal in the row B or A, etc., are all included in the protection scope of the present invention.
Claims (14)
1. Adjustable CO reformed from in-line type decomposing furnace2Enrichment cement kiln system, its characterized in that, cement kiln system includes: the device comprises a first row of cyclone preheaters, a second row of cyclone preheaters, a third row of cyclone preheaters, a first decomposing furnace, a second decomposing furnace, a smoke chamber, a rotary kiln and a cooler;
the air inlets of the first row of cyclone preheaters and the second row of cyclone preheaters are connected with the first decomposing furnace; the discharge port of the first row of cyclone preheaters or the discharge port of the second row of cyclone preheaters is connected with the second decomposing furnace; the air inlet of the third row of cyclone preheaters is connected with the second decomposing furnace, and the discharge hole of the first-to-last cyclone separator of the third row of cyclone preheaters is connected with the smoke chamber;
the first decomposing furnace is connected with a smoke chamber, and the smoke chamber is connected with the rotary kiln; the rotary kiln is connected with a cooler;
a first distributing valve is arranged at a discharging pipe of a penultimate cyclone separator of the second row of cyclone preheaters, one end of the first distributing valve is connected with the first decomposing furnace, and the other end of the first distributing valve is connected with the second decomposing furnace.
2. The adjustable CO retrofitted to in-line decomposition furnace of claim 12The enrichment cement kiln system is characterized in that a penultimate cyclone separator of a first row of cyclone preheaters is connected with a first decomposing furnace through a pipeline, and the pipeline does not comprise a branch or comprises a branch;
when the pipeline does not comprise a branch, the first row of cyclone preheaters feeds the first decomposing furnace at a single point;
when the pipeline comprises a branch, the first row of cyclone preheaters feeds the first decomposing furnace at multiple points; the pipeline comprises a conveying main road and conveying branch roads, the number of the conveying branch roads is more than 2, the conveying branch roads are connected in parallel, and a second distributing valve is arranged at the joint of the conveying main road and the conveying branch roads; the second material distribution valve is used for adjusting the material quantity entering the conveying branch from the conveying main path.
3. The adjustable CO retrofitted to in-line decomposition furnace of claim 12The enrichment cement kiln system is characterized in that the series of the first row of cyclone preheaters and the series of the second row of cyclone preheaters are selected from 3-7 stages;
the number of stages of the third row of cyclone preheaters is 1-5.
4. The adjustable CO retrofitted to in-line decomposition furnace of claim 12The enrichment cement kiln system is characterized in that the cooler is one of a grate cooler, a single-cylinder cooler and a multi-cylinder cooler;
the cement kiln system also comprises a tertiary air pipe; one end of the tertiary air pipe is connected with the cooler, and the other end of the tertiary air pipe is connected with the first decomposing furnace.
5. The adjustable CO retrofitted to in-line decomposition furnace of claim 12The cement kiln system with the enrichment amount is characterized by further comprising a cooler, wherein an air outlet of the third row of cyclone preheaters is connected with the cooler; and the cooler is used for cooling the flue gas discharged from the air outlet of the third row of cyclone preheaters.
6. The adjustable CO retrofitted to in-line decomposition furnace of claim 32The enrichment cement kiln system is characterized in that the first row of cyclone preheaters and the second row of cyclone preheaters are provided with feed inlets, and the feed inlets are arranged at inlet air pipes of uppermost first-stage cyclone separators of the first row of cyclone preheaters and the second row of cyclone preheaters or at inlet air pipes of uppermost second-stage cyclone separators of the first row of cyclone preheaters and the second row of cyclone preheaters;
the third row of the cyclone preheaters are provided with or not provided with feed inlets;
when the stage number of the third row of the cyclone preheaters is 1 stage, no feeding hole is arranged on the third row of the cyclone preheaters;
when the number of stages of the third row of cyclone preheaters is more than 2, a feeding hole is formed in the third row of cyclone preheaters; the feed inlet of the third row of cyclone preheaters is arranged at the inlet air pipe of the uppermost first-stage cyclone separator of the third row of cyclone preheaters or at the inlet air pipe of the uppermost second-stage cyclone separator of the third row of cyclone preheaters.
7. The adjustable CO retrofitted to in-line decomposition furnace of claim 62The enriched quantity cement kiln system is characterized in that when the grade number of the third row of cyclone preheaters is more than 2 grades, a communicating pipeline is arranged between the third row of cyclone preheaters and the first row of cyclone preheaters, and/or a communicating pipeline is arranged between the third row of cyclone preheaters and the second row of cyclone preheaters; the communicating pipeline is used for conveying the raw meal preheated by the third row of cyclone preheaters to the first row of cyclone preheaters or the second row of cyclone preheaters or simultaneously conveying the raw meal to the first row of cyclone preheaters and the second row of cyclone preheaters;
one end of the communicating pipeline is arranged at a discharge port of a last but one second cyclone separator of the third row of cyclone preheaters;
the other end of the communicating pipeline is arranged on an inlet air pipe of a first-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater, or on an inlet air pipe of a second-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater, or on an inlet air pipe of a third-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater, or on an inlet air pipe of a fourth-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater, or on an inlet air pipe of a fifth-stage cyclone separator on the top of the first-column cyclone preheater or the second-column cyclone preheater.
8. The adjustable CO retrofitted to the in-line decomposition furnace of claim 42The cement kiln system with the enrichment amount is characterized by further comprising a heat exchanger, the tertiary air pipe is divided into two paths, and the tertiary air pipeOne end of the first decomposition furnace is connected with a cooling machine, and the other end of one path of the third air pipe is connected with a first decomposition furnace; the other path is a tertiary air pipe, the other end of the tertiary air pipe is connected with a heat exchanger, and the heat exchanger is connected with a second decomposing furnace through a pipeline.
9. Use of the adjustable CO retrofitted on the in-line decomposition furnace according to any of claims 1 to 82A method of producing cement clinker in an enriched quantity cement kiln system, the method comprising:
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 meal preheated by the first row of cyclone preheaters and the second row of cyclone preheaters enters the first decomposing furnace through one or more points; part of the hot raw meal preheated by the first row of cyclone preheaters or the second row of cyclone preheaters or the first row of cyclone preheaters and the second row of cyclone preheaters enters the second decomposing furnace through one point or multiple points;
the decomposed hot raw materials leave the first decomposing furnace and the second decomposing furnace, are separated from the flue gas and then enter the rotary kiln, are calcined in the rotary kiln to form cement clinker, and the clinker enters a cooling machine from the outlet of the rotary kiln;
the mixed gas of oxygen and circulating flue gas or oxygen is conveyed into a second decomposition furnace, the second decomposition furnace is oxygen-enriched combustion or total oxygen combustion, and high CO generated in the second decomposition furnace2The concentrated flue gas is discharged through a third row of cyclone preheaters; the CO can be regulated by regulating the amount of hot raw meal entering the second decomposition furnace2And (4) enriching amount.
10. The method for manufacturing cement clinker according to claim 9, wherein the raw meal preheated by the second row of cyclone preheaters is divided into two paths by the first material dividing valve, one path enters the first decomposing furnace, and the other path enters the second decomposing furnace;
the amount of hot raw meal fed into the second decomposing furnace through the first material distributing valve can be adjusted to adjust CO2And (4) enriching amount.
11. The method for manufacturing cement clinker according to claim 10,
respectively feeding raw materials into a first row of cyclone preheaters and a second row of cyclone preheaters, enabling the raw materials preheated by the first row of cyclone preheaters and the second row of cyclone preheaters to enter a first decomposing furnace, adjusting the quantity of the hot raw materials conveyed into a second decomposing furnace through a first material distributing valve, enabling the second decomposing furnace to be in oxygen-enriched combustion or total oxygen combustion, and enabling the system to be CO2The self-enrichment type pre-decomposition kiln can adjust the amount of the hot raw materials entering the second decomposition furnace through adjusting the first material distributing valve2Enriching amount;
raw materials are respectively fed into a first row of cyclone preheaters and a second row of cyclone preheaters, the raw materials preheated by the first row of cyclone preheaters and the second row of cyclone preheaters enter a first decomposing furnace, a first material distributing valve is adjusted to enable all the raw materials preheated by the second row of cyclone preheaters to be conveyed to the first decomposing furnace, the second decomposing furnace, the third row of cyclone preheaters and a cooler are stopped to be used, and at the moment, the system is a conventional online type pre-decomposing kiln.
12. Method for manufacturing cement clinker according to claim 9, wherein when the raw meal is fed to the third row of cyclone preheaters, the preheated raw meal from the third row of cyclone preheaters is fed to the first row of cyclone preheaters or the second row of cyclone preheaters through the connecting duct or to both the first row of cyclone preheaters and the second row of cyclone preheaters.
13. The method for preparing cement clinker according to claim 9, wherein the air is cooled by the cooler in terms of gas flow direction, and the heat exchange is completed by the air comprising 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; the second path of high-temperature air is used as tertiary air and directly enters the first decomposing furnace for fuel combustion; and the third path of air with higher temperature enters a waste heat boiler for power generation or other waste heat utilization or treatment systems, and the flue gas after power generation is completed or other waste heat utilization or treatment systems is treated by the waste air and then is discharged into the atmosphere through a chimney.
14. The method for preparing cement clinker according to claim 13, wherein the second path of high temperature air is divided into two paths as tertiary air, wherein one path of tertiary air enters the first decomposing furnace through a tertiary air pipe; the other path of tertiary air enters a heat exchanger through a tertiary air pipe, the mixed gas of oxygen and circulating flue gas or oxygen enters the heat exchanger, the mixed gas of oxygen and circulating flue gas or oxygen after heat exchange enters a second decomposition furnace through a pipeline, and oxygen-enriched combustion or total oxygen combustion is carried out in the second decomposition furnace; the tertiary air after heat exchange enters a waste heat utilization or treatment system;
the waste heat utilization or treatment system comprises waste heat power generation and material drying.
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| CN115682747A (en) * | 2022-11-14 | 2023-02-03 | 南京凯盛国际工程有限公司 | Carbon dioxide enrichment system of gradient combustion off-line decomposing furnace and process principle thereof |
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