CN115159876B - Low-energy-consumption carbon-trapping cement clinker production system and cement clinker preparation method - Google Patents
Low-energy-consumption carbon-trapping cement clinker production system and cement clinker preparation method Download PDFInfo
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- CN115159876B CN115159876B CN202210759027.3A CN202210759027A CN115159876B CN 115159876 B CN115159876 B CN 115159876B CN 202210759027 A CN202210759027 A CN 202210759027A CN 115159876 B CN115159876 B CN 115159876B
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- 239000004568 cement Substances 0.000 title claims abstract description 59
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 33
- 238000005265 energy consumption Methods 0.000 title claims abstract description 22
- 238000002360 preparation method Methods 0.000 title description 2
- 239000003546 flue gas Substances 0.000 claims abstract description 104
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 103
- 238000000034 method Methods 0.000 claims abstract description 37
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 24
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 24
- 239000002918 waste heat Substances 0.000 claims description 48
- 238000002485 combustion reaction Methods 0.000 claims description 42
- 239000000446 fuel Substances 0.000 claims description 36
- 238000000926 separation method Methods 0.000 claims description 28
- 239000000779 smoke Substances 0.000 claims description 22
- 239000000428 dust Substances 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 19
- 238000013461 design Methods 0.000 abstract description 12
- 239000003517 fume Substances 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 description 36
- 239000007787 solid Substances 0.000 description 24
- 235000012054 meals Nutrition 0.000 description 23
- 239000001301 oxygen Substances 0.000 description 21
- 229910052760 oxygen Inorganic materials 0.000 description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 20
- 238000005516 engineering process Methods 0.000 description 17
- 238000000354 decomposition reaction Methods 0.000 description 16
- 238000005245 sintering Methods 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- 230000009467 reduction Effects 0.000 description 4
- 238000011160 research Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000010304 firing Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000003746 solid phase reaction Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 229920003169 water-soluble polymer Polymers 0.000 description 1
Classifications
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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
- C04B7/364—Avoiding environmental pollution during cement-manufacturing
- C04B7/367—Avoiding or minimising carbon dioxide emissions
-
- 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
- C04B7/434—Preheating with addition of fuel, e.g. calcining
-
- 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
- C04B7/44—Burning; Melting
- C04B7/4407—Treatment or selection of the fuel therefor, e.g. use of hazardous waste as secondary fuel ; Use of particular energy sources, e.g. waste hot gases from other processes
Abstract
The application belongs to the technical field of cement clinker production, and particularly relates to a low-energy-consumption carbon-trapping cement clinker production system and a method for preparing cement clinker. The application provides a method for improving CO in flue gas 2 Concentration, simplified technological process of fume trapping and purifying system, system design, low energy consumption carbon trapping and cement clinker producing system with less modifying work and cement clinker preparing process.
Description
Technical Field
The application belongs to the technical field of cement production, and particularly relates to a low-energy-consumption carbon-trapping cement clinker production system and a method for preparing cement clinker.
Background
The researches on carbon emission reduction technology are not reported at home and abroad, but the researches are mainly oriented to industries such as electric power, coal, steel and the like, and the reports on carbon emission reduction related technology in the cement industry are relatively less. The current cement production process is a novel dry production process which mainly comprises a cooler, a burner, a rotary kiln, a decomposing furnace, a cyclone preheater and the like. Wherein, raw meal is preheated and heated in a cyclone preheater, decomposed in a decomposing furnace, most of fuel is combusted in the decomposing furnace to provide heat required by raw meal decomposition, decomposed materials are continuously calcined in a rotary kiln to generate cement clinker, and then the cement clinker is cooled to a proper temperature by a cooler.
However, the present inventors have found that the above prior art has at least the following technical problems:
currently, combustion-supporting medium introduced into a cement kiln system is air, and CO in flue gas at the outlet of a cyclone preheater 2 The concentration is generally 20-30%. As shown in figure 1 of the specification, the novel dry-method cement clinker firing system mainly comprises a waste heat utilization system, a cyclone preheater, a decomposing furnace, a kiln tail smoke chamber, a rotary kiln, a kiln head burner, a clinker cooler and the like, and the specific production process flow is as follows: the raw meal is fed into a preheater system through the top of the cyclone preheater, is subjected to gas-solid heat exchange through the multi-stage cyclone preheater, then is calcined and decomposed in a decomposing furnace, is subjected to gas-solid separation through the cyclone preheater, is then fed into a kiln tail smoke chamber, is then fed into a rotary kiln for solid-phase reaction sintering to generate clinker, and is then cooled by a clinker cooler to obtain cement clinker. The air cools the high-temperature clinker through the cooler, and the air after heat exchange is mainly divided into the following three paths: the first path of high-temperature air is taken as secondary air to directly enter the rotary kiln for fuel combustion, and kiln gas formed by combustion of the fuel in the rotary kiln and decomposition of part of raw materials enters a decomposing furnace; the second path of high-temperature air is taken as tertiary air and enters the decomposing furnace through a tertiary air pipe for fuel combustion; the third path of air with higher temperature enters the waste heat boiler to generate power or perform other forms of waste heat utilization, and the air after the waste heat utilization is discharged into the atmosphere after being processed by the flue gas treatment system. The flue gas generated by combustion of fuel in the decomposing furnace and decomposition of raw meal leaves the decomposing furnace to enter a cyclone preheater in a row A and a cyclone preheater in a row B respectively, then the raw meal in the row A and the raw meal in the row B are preheated for multiple times and separated from gas and solid, and finally the flue gas leaves from outlets of the cyclone preheaters in the row A and the cyclone preheaters in the row B and the cyclone preheaters in the row A and the cyclone preheaters in the row B respectivelyExiting flue gas CO 2 The concentration is 20-30%. And (3) recovering part of heat from high-temperature waste gas discharged from outlets of the cyclone preheaters in the A column and the B column by a waste heat recovery system, feeding the waste gas into a raw material grinding system to dry raw materials, feeding the raw materials into a smoke treatment system, and discharging the raw materials into the atmosphere after the raw materials are treated by the smoke treatment system.
The prior carbon emission reduction technical proposal adopted by the cement industry mainly comprises a pre-combustion trapping, a post-combustion trapping or a cement kiln total oxygen combustion technology. Wherein the pre-combustion trapping means that the fuel is pretreated before combustion, and carbon in the fuel is separated. Due to the technical characteristics of cement clinker production, CO before combustion 2 One significant disadvantage of trapping is that only the CO produced by the combustion of the fuel can be separated 2 While the raw meal is calcined to produce CO 2 (about CO) 2 60% of the total emissions are emitted with the flue gases, this part of the CO 2 Without any treatment. In addition, the pre-combustion capture technology compares to other CO 2 The condition of hydrogen combustion in the clinker calcination process of the trapping technology is very harsh, and the special design of the rotary kiln burner is needed, so that the technology has low feasibility in the cement industry and can be eliminated. The post-combustion trapping technology mainly aims at trapping the burnt flue gas or separating CO 2 The main techniques include absorption, adsorption, membrane separation, mineral carbonization, and the like. Due to the small pressure, large volume flow and CO of the kiln tail gas in the cement industry 2 Low in concentration and contains a large amount of dust and N 2 The method has the problems of low carbon trapping efficiency, small trapping flow, complex system, large equipment investment or high running cost.
The cement kiln total oxygen combustion technology is to replace air with high-purity oxygen (the oxygen purity is generally 90-95%) to support combustion, so that the CO of the flue gas at the outlet of the kiln tail preheater can be greatly improved 2 Concentration and further greatly save the subsequent flue gas CO 2 Investment costs and operating costs of the capture purification system. The cement kiln oxy-fuel combustion technology can be subdivided into a full-system oxy-fuel combustion technology and a decomposing furnace oxy-fuel combustion technology, wherein the full-system oxy-fuel combustion technology relates to the oxy-fuel combustion technology adopted in the rotary kiln and the decomposing furnace, and a cooler, a main burner and the decomposing furnace need to be consideredKey equipment of the firing system is subjected to key design, and the change amount of the existing firing system is large; the decomposing furnace total oxygen combustion technology only considers that the decomposing furnace adopts the total oxygen combustion technology, only needs to carry out key design on the decomposing furnace, has small change amount on the existing sintering system, is a key research direction of carbon emission reduction in the cement industry at the present stage, but the existing research or published decomposing furnace total oxygen combustion technology generally has the defects of small treatment smoke amount, high system energy consumption and the like.
Difficulty and meaning for solving the technical problems:
thus, based on these problems, a method for improving CO in flue gas is provided 2 The concentration, the process flow of the flue gas capturing and purifying system is simplified, the system design is realized, and the low-energy-consumption carbon capturing cement clinker production system with small reconstruction workload and the method for preparing the cement clinker have important practical values.
Disclosure of Invention
The application aims to solve the technical problems in the prior art and provide a method for improving CO in flue gas 2 Concentration, simplified technological process of fume trapping and purifying system, system design, low energy consumption carbon trapping and cement clinker producing system with less modifying work and cement clinker preparing process.
The technical scheme adopted by the embodiment of the application for solving the technical problems in the prior art is as follows:
the low-energy-consumption carbon-trapping cement clinker production system comprises a cooler, a rotary kiln, a smoke chamber, a decomposing furnace, an A-column cyclone preheater, a B-column cyclone preheater and a C-column cyclone preheater, wherein discharging pipes of the A-column cyclone preheater, the B-column cyclone preheater and the C-column cyclone preheater are connected with a feeding port of the decomposing furnace, an outlet of the decomposing furnace is connected with an air inlet of the A-column lowest-stage cyclone preheater, a discharging pipe of the A-column lowest-stage cyclone preheater is connected with the smoke chamber, the smoke chamber is not directly communicated with the decomposing furnace, and the smoke chamber, the rotary kiln and the cooler are sequentially connected.
The embodiment of the application can also adopt the following technical scheme:
in the low-energy-consumption carbon-trapping cement clinker production system, further, the first-last cyclone preheater in the A column, the second-last cyclone preheater in the B column and the second-last cyclone preheater in the C column are connected with a feeding pipe of the decomposing furnace.
In the low-energy-consumption carbon-trapping cement production system, further, the number of the cyclone preheater in the A column is three to seven, the number of the cyclone preheater in the B column is three to seven, and the number of the cyclone preheater in the C column is three to seven.
In the low-energy-consumption carbon-trapping cement clinker production system, further, the flue gas discharged from the decomposing furnace enters the cyclone preheater A, the flue gas leaving the cyclone preheater A is divided into two paths, and after one path of flue gas is mixed with high-purity oxygen prepared by the air separating device according to a certain proportion, the mixed gas enters the bottom of the decomposing furnace; the other path of flue gas is cooled by a heat exchanger, the cooled flue gas is subjected to flue gas dust removal by a dust remover, and the dust removed flue gas enters CO 2 And (5) capturing and purifying the system.
In the low-energy-consumption carbon-trapping cement clinker production system, further, O in the mixed gas 2 The volume ratio of the water-soluble polymer is 20-80%.
In the low-energy-consumption carbon-trapping cement clinker production system, further, the air leaving from the outlet of the C-column cyclone preheater is divided into two paths, wherein one path of air enters the waste heat utilization system, the other path of air enters the heat exchanger system through the circulating fan, indirect heat exchange is carried out on the air and the mixed gas in the heat exchanger system, and the air enters the waste heat utilization system after heat exchange is finished.
In the low-energy-consumption carbon-trapped cement clinker production system, further, the high-temperature air discharged from the cooler is divided into three paths, and the air in the first path is taken as secondary air to directly enter the rotary kiln for fuel combustion, and enters the B-column cyclone preheater through the air inlet of the B-column lowest-stage cyclone preheater; the second path of air enters the C-column cyclone preheater through the air inlet of the lowest stage cyclone preheater in the C-column; the third air enters a waste heat utilization system, and after the waste heat is utilized, the waste heat is treated by a flue gas treatment system and then discharged into the atmosphere.
In the low-energy-consumption carbon-trapped cement clinker production system, the temperature of the first air is 950-1200 ℃; the temperature of the second path of air is 850-1000 ℃; the temperature of the third air path is 250-450 ℃.
In the low-energy-consumption carbon-trapping cement clinker production system, further, the flue gas discharged from the cyclone preheater B enters a waste heat utilization system, and after the waste heat is utilized, the flue gas is treated by a flue gas treatment system and then discharged into the atmosphere; and the air which is discharged from the C-column cyclone preheater enters a waste heat utilization system, and is discharged to the atmosphere after being treated by a flue gas treatment system after being utilized by waste heat.
A method of preparing cement clinker using low energy carbon capture using the low energy carbon capture cement clinker production system of any of the above.
One or more technical solutions provided in the embodiments of the present application have at least the following beneficial effects:
1. CO in flue gas at outlet of preheater of existing sintering system 2 Concentration of 20-30%, purification of 99.9% industrial grade or 99.99% food grade or dry ice form CO 2 The process flow required by the product is complex, and the investment cost and the operation cost of the trapping and purifying system are high. The decomposing furnace outlet is connected with the cyclone preheater in the A column, and O is arranged in the decomposing furnace 2 /CO 2 Atmosphere capable of realizing the flue gas CO at the outlet of the cyclone preheater in row A 2 The concentration is more than or equal to 75 percent (dry basis concentration), and CO in the flue gas 2 The concentration is improved, so that the process flow of the flue gas capturing and purifying system can be simplified, and the investment cost and the operation cost of the flue gas capturing and purifying system are obviously reduced.
2. If CO is generated for the existing sintering system 2 When all the materials are collected and purified, the whole burning system needs to be designed into a total oxygen burning mode, and a decomposing furnace, a main burner and a cooler need to be designed in a key way at the same time, so that the project design or the transformation workload is large. The application creatively changes the existing burning system into an off-line type, namely, the smoke chamber and the decomposing furnace are designed to be disconnected, based on the design, the design intention of the decomposing furnace for full-oxygen combustion can be realized by only slightly reforming the decomposing furnace, and the system design or reforming workload is small.
3. The tertiary air pipe of the existing cement production line is connected with the decomposing furnace, the tertiary air enters the decomposing furnace through the tertiary air pipe to support combustion, and the heat recovery efficiency of the system is effectively guaranteed through the design of the tertiary air. Because the cooler still adopts air cooling, tertiary air is high-temperature air, if the cooler still adopts a tertiary air pipe to be connected with the decomposing furnace, CO in flue gas at the outlet of the decomposing furnace can be obviously reduced due to the existence of a large amount of nitrogen in the air 2 The concentration of the raw meal in the C column is fully preheated by the original high-temperature air in the C column cyclone preheater while the tertiary air pipe is canceled, the raw meal after fully heat exchange is decomposed in the decomposing furnace, and the air after fully heat exchange can be fed into the waste heat recovery system or the mixed flue gas preheated in the oxy-fuel combustion decomposing furnace as required, namely, CO in the flue gas at the outlet of the A column cyclone preheater is ensured 2 The concentration is more than or equal to 75 percent (dry basis concentration), the heat recovery efficiency of a sintering system is not reduced, and the economy of the technical scheme is improved.
4. The method comprises the steps that raw materials fed into a decomposing furnace are fully preheated through independent row preheaters, the number of stages (such as 4 stages or 5 stages) of row C is reasonably designed, first, the second path of high-temperature air is cooled to a reasonable temperature of 300-450 ℃, and then mixed flue gas is preheated through a circulating fan heat feeding exchanger; or the series of the C column is designed to be 6 or higher, the temperature of the second path of flue gas is directly reduced to about 240 ℃, and then the flue gas enters a waste heat utilization system. The two technical schemes can effectively ensure that the heat recovery efficiency of the sintering system is not reduced.
Drawings
The technical solution of the embodiments of the present application will be described in further detail below with reference to the accompanying drawings, but it should be understood that these drawings are designed for the purpose of illustration only and thus are not limiting of the scope of the present application. Moreover, unless specifically indicated otherwise, the drawings are intended to conceptually illustrate the structural configurations described herein and are not necessarily drawn to scale.
FIG. 1 is a prior art process flow diagram;
FIG. 2 is a process flow diagram of a first embodiment of the application;
fig. 3 is a process flow diagram of a second embodiment of the present application.
In the figure: 1. smoke chamber, 2, decomposing furnace, 3, A column cyclone preheater, 4, B column cyclone preheater, 5, C column cyclone preheater, 6, rotary kiln, 7, air separator, 8, heat exchanger system, 9, heat exchanger, 10, dust remover, 11, cooler.
Detailed Description
The application mixes the high-purity oxygen with the circulating smoke, and the mixed smoke enters the decomposing furnace to form O in the decomposing furnace 2 /CO 2 Atmosphere, and then CO in the mixed smoke product obtained by combustion of fuel in the decomposing furnace and decomposition of raw materials 2 The concentration is more than or equal to 75 percent (dry basis concentration), thereby realizing CO 2 The concentration is self-enriched in the decomposing furnace, and the flue gas CO 2 The concentration is obviously improved, and the CO can be effectively improved 2 Efficiency of the trapping and purifying system, thereby realizing CO 2 The operation cost of the trapping and purifying system is obviously reduced, namely the technology can provide a low-energy-consumption carbon trapping cement clinker production system and a method for preparing cement clinker.
In order to better understand the above technical solutions, the following detailed description will refer to the accompanying drawings and specific embodiments.
Example 1
The embodiment mainly comprises the process flow shown in fig. 2:
according to the material flow direction, raw materials are respectively fed into cyclone preheaters of the A column, the B column and the C column of the pre-decomposition kiln through a feeding device by a lifting machine, heat exchange is carried out with smoke in the cyclone separator of the cyclone preheaters and a connecting air pipe, and the smoke is separated in the cyclone separator. Raw materials in the A row enter a decomposing furnace from a second-last cyclone separator in the A row after multiple heat exchange and gas-solid separation, raw materials in the B row enter the decomposing furnace from a last cyclone separator in the B row after multiple heat exchange and gas-solid separation, and raw materials in the C row enter the decomposing furnace from a last cyclone separator in the C row after multiple heat exchange and gas-solid separation. The fuel in the decomposing furnace burns to release a large amount of heat for decomposing the raw meal, the decomposed raw meal leaves the decomposing furnace and enters the rotary kiln after being subjected to gas-solid separation by the cyclone separator at the lowest stage of the A column, the raw meal is continuously calcined in the rotary kiln to generate clinker, and the clinker falls into a cooler from a kiln mouth of the rotary kiln and is cooled to 65 ℃ plus environmental temperature by the cooler.
According to the gas flow direction, the air cools the high-temperature clinker by a cooler, and the air subjected to heat exchange is mainly divided into the following three paths: the first path of high-temperature air is taken as secondary air to directly enter the rotary kiln for fuel combustion, kiln gas formed by combustion of the rotary kiln and decomposition of part of raw materials enters the B-row cyclone preheater through a connecting air pipe of the B-row lowest-stage cyclone separator, and then the B-row raw materials are preheated for a plurality of times and subjected to gas-solid separation and finally leave from an outlet of the B-row cyclone preheater. Flue gas CO exiting from a B-bank cyclone preheater 2 The concentration is less than or equal to 15 percent, and then the flue gas enters a waste heat utilization system, and the flue gas after waste heat utilization is discharged to the atmosphere after being treated by a flue gas treatment system; the second path of high-temperature air enters the C-column lowest-stage cyclone preheater through the kiln door cover, then the C-column raw material is preheated for a plurality of times and subjected to gas-solid separation, and finally leaves from the outlet of the C-column cyclone preheater, then the air enters the waste heat utilization system, and the air after waste heat utilization is treated by the flue gas treatment system and is discharged into the atmosphere; the third path of air with higher temperature enters the waste heat boiler to generate power or perform other forms of waste heat utilization, and the air after the waste heat utilization is discharged into the atmosphere after being processed by the flue gas treatment system. The high-purity oxygen prepared by the air separation device and the part of the circulating smoke of the A column are mixed according to a certain proportion and then enter the bottom of the decomposing furnace to burn the fuel entering the decomposing furnace. The fuel combustion and the raw material decomposition in the decomposing furnace release a large amount of CO 2 Then the flue gas generated by combustion of fuel in the decomposing furnace and decomposition of raw meal leaves the decomposing furnace to enter an A-row cyclone preheater, then the A-row raw meal is preheated and gas-solid separated for multiple times, and finally leaves from the outlet of the A-row cyclone preheater, and the flue gas CO leaves from the A-row cyclone preheater 2 The concentration is more than or equal to 75% (dry basis concentration), then the flue gas is divided into two paths, wherein one path of flue gas is mixed with high-purity oxygen prepared by an air separation device according to a certain proportion and then enters the bottom of the decomposing furnace for burning fuel entering the decomposing furnace. The other path of flue gas is cooled by a heat exchanger, the cooled flue gas is subjected to flue gas dust removal by a dust remover, and the dust removed flue gas enters CO 2 Trapping and purifying system, and CO after further trapping and purifying process 2 The concentration can reach more than 99 percent, and the method can be sealed or recycled.
The preferred number of the A-column cyclone preheater is three-seven;
the preferred number of the B-column cyclone preheater is three-seven;
the preferred number of the C-column cyclone preheater is three-seven;
the preferable temperature of the first path of air is 950-1200 ℃;
the preferable temperature of the second air is 850-1000 ℃;
the preferable temperature of the third air path is 250-450 ℃;
the cooling process can be used for cooling by taking air or cooling water as a cooling medium;
the high-purity oxygen can also be obtained by outsourcing;
o in the mixed gas mixed according to a certain proportion 2 With CO 2 The ratio of the oxygen to the oxygen in the mixed gas can be adjusted according to the heat value of the fuel and the required operation temperature in the decomposing furnace 2 The volume ratio is preferably 20-80%.
The principle of the application is as follows:
in the process, as shown in fig. 2, raw materials are fed into cyclone preheaters of a pre-decomposition kiln A, B and C respectively through a feeding device by a lifting machine, heat exchange is carried out with flue gas in the cyclone separator of the cyclone preheater and a connecting air pipe, and finally the raw materials can be preheated to 700-800 ℃ and separated from the flue gas in the cyclone separator. Raw materials in the A row enter a decomposing furnace from a second-last cyclone separator in the A row after multiple heat exchange and gas-solid separation, raw materials in the B row enter the decomposing furnace from a last cyclone separator in the B row after multiple heat exchange and gas-solid separation, and raw materials in the C row enter the decomposing furnace from a last cyclone separator in the C row after multiple heat exchange and gas-solid separation. The fuel in the decomposing furnace burns to release a large amount of heat for decomposing the raw meal, the raw meal leaves the decomposing furnace, enters the rotary kiln after being separated by gas and solid by the cyclone separator at the lowest stage of the A column, is continuously calcined in the rotary kiln to generate clinker,the clinker falls from the kiln opening of the rotary kiln into a cooler, and is cooled to 65 ℃ plus the ambient temperature by the cooler. The air cools the high-temperature clinker through the cooler, and the air after heat exchange is mainly divided into the following three paths: the first path of high-temperature air is taken as secondary air to directly enter the rotary kiln for fuel combustion, kiln gas formed by combustion of the rotary kiln and decomposition of part of raw materials enters the B-row cyclone preheater through a connecting air pipe of the B-row lowest-stage cyclone separator, and then the B-row raw materials are preheated for a plurality of times and subjected to gas-solid separation and finally leave from an outlet of the B-row cyclone preheater. Flue gas CO exiting from a B-bank cyclone preheater 2 The concentration is less than or equal to 15 percent, and then the flue gas enters a waste heat utilization system, and the flue gas after waste heat utilization is discharged to the atmosphere after being treated by a flue gas treatment system; the second path of high-temperature air enters a C-column cyclone preheater through a kiln door cover, then the C-column raw material is preheated for a plurality of times and subjected to gas-solid separation, and finally leaves from an outlet of the C-column cyclone preheater, then the air enters a waste heat utilization system, and the air after waste heat utilization is treated by a flue gas treatment system and is discharged into the atmosphere; the third path of air with higher temperature enters the waste heat boiler to generate power or perform other forms of waste heat utilization, and the air after the waste heat utilization is discharged into the atmosphere after being processed by the flue gas treatment system. The high-purity oxygen prepared by the air separation device or purchased by the air separation device is mixed with part of the circulating smoke of the column A according to a certain proportion and then enters the bottom of the decomposing furnace to burn the fuel entering the decomposing furnace. The fuel combustion and the raw material decomposition in the decomposing furnace release a large amount of CO 2 Then the flue gas generated by combustion of fuel in the decomposing furnace and decomposition of raw meal leaves the decomposing furnace to enter an A-row cyclone preheater, then the A-row raw meal is preheated and gas-solid separated for multiple times, and finally leaves from the outlet of the A-row cyclone preheater, and the flue gas CO leaves from the A-row cyclone preheater 2 The concentration is more than or equal to 75% (dry basis concentration), then the flue gas is divided into two paths, wherein one path of flue gas is mixed with high-purity oxygen prepared by an air separation device or purchased externally according to a certain proportion and then enters the bottom of the decomposing furnace for burning the fuel entering the decomposing furnace. The other path of flue gas is cooled by a heat exchanger, the cooled flue gas is subjected to flue gas dust removal by a dust remover, and the dust removed flue gas enters CO 2 Trapping and purifying system, and CO after further trapping and purifying process 2 The concentration can reach 99 percentAnd the method can be used for sealing or recycling.
Example 2
As shown in fig. 3, the homogenized raw materials are respectively fed into a pre-decomposition kiln system A, B and C by a raw material hoister, the raw materials are subjected to multiple heat exchange with flue gas by a cyclone separator and a connecting air pipe, and finally the raw materials can be preheated to 700-800 ℃; raw materials in the A row enter a decomposing furnace from a second-last cyclone separator in the A row after multiple heat exchange and gas-solid separation, raw materials in the B row enter the decomposing furnace from a last cyclone separator in the B row after multiple heat exchange and gas-solid separation, and raw materials in the C row enter the decomposing furnace from a last cyclone separator in the C row after multiple heat exchange and gas-solid separation. The fuel in the decomposing furnace burns to release a large amount of heat for decomposing the raw meal, the decomposed raw meal leaves the decomposing furnace and enters the rotary kiln after being subjected to gas-solid separation by the cyclone separator at the lowest stage of the A column, the raw meal is continuously calcined in the rotary kiln to generate clinker, and the clinker falls into a cooler from a kiln mouth of the rotary kiln and is cooled to 65 ℃ plus environmental temperature by the cooler. The air cools the high-temperature clinker through the cooler, and the air after heat exchange is mainly divided into the following three paths: the first path of high-temperature air is taken as secondary air to directly enter the rotary kiln for fuel combustion, kiln gas formed by combustion of the rotary kiln and decomposition of part of raw materials enters the B-row cyclone preheater through a connecting air pipe of the B-row lowest-stage cyclone separator, and then the B-row raw materials are preheated for a plurality of times and subjected to gas-solid separation and finally leave from an outlet of the B-row cyclone preheater. Flue gas CO exiting from a B-bank cyclone preheater 2 The concentration is less than or equal to 15 percent, and then the flue gas enters a waste heat utilization system, and the flue gas after waste heat utilization is discharged to the atmosphere after being treated by a flue gas treatment system; the second path of high-temperature air enters the C-column cyclone preheater through the kiln door cover, then the C-column raw material is preheated for a plurality of times and subjected to gas-solid separation, and finally leaves from the outlet of the C-column cyclone preheater, the air leaving from the outlet of the C-column cyclone preheater is divided into two paths, one path of air enters the waste heat utilization system, and the air after waste heat utilization is discharged to the atmosphere after being treated by the flue gas treatment system. The second path of air enters the heat exchanger system through the circulating fan, and indirect heat exchange is carried out on the second path of air and the mixed flue gas which is prepared by the air separation device or is composed of outsourced high-purity oxygen and part of circulating flue gas in the A column and is arranged in the heat exchanger system (namely, the second path of airThe gas is not in direct contact with the mixed flue gas), the mixed flue gas after heat exchange enters the bottom of the decomposing furnace, the air after heat exchange enters the waste heat utilization system, and the air after waste heat utilization is treated by the flue gas treatment system and then is discharged into the atmosphere; the third path of air with higher temperature enters the waste heat boiler to generate power or perform other forms of waste heat utilization, and the air after the waste heat utilization is discharged into the atmosphere after being processed by the flue gas treatment system. The high-purity oxygen prepared or purchased by the air separation device is mixed with part of the circulating flue gas in the row A according to a certain proportion and then enters a heat exchanger system to exchange heat with the second path of high-temperature air from the cooler, and the mixed flue gas after heat exchange enters the bottom of the decomposing furnace to be burnt by fuel entering the decomposing furnace. The fuel combustion and the raw material decomposition in the decomposing furnace release a large amount of CO 2 Then the flue gas generated by combustion of fuel in the decomposing furnace and decomposition of raw meal leaves the decomposing furnace to enter an A-row cyclone preheater, then the A-row raw meal is preheated and gas-solid separated for multiple times, and finally leaves from the outlet of the A-row cyclone preheater, and the flue gas CO leaves from the A-row cyclone preheater 2 The concentration is more than or equal to 75% (dry basis concentration), then the flue gas is divided into two paths, one path of flue gas is mixed with high-purity oxygen prepared or purchased by an air separation device according to a certain proportion and then enters a heat exchanger system for heat exchange, and the mixed flue gas after heat exchange enters the bottom of the decomposing furnace for burning fuel entering the decomposing furnace. The other path of flue gas is cooled by a heat exchanger, the cooled flue gas is subjected to flue gas dust removal by a dust remover, and the dust removed flue gas enters CO 2 Trapping and purifying system, and CO after further trapping and purifying process 2 The concentration can reach more than 99 percent, and the method can be sealed or recycled.
In summary, the present application provides a method for increasing CO in flue gas 2 Concentration, simplified technological process of fume trapping and purifying system, system design, low energy consumption carbon trapping cement producing system with less reconstruction work load and process of preparing cement clinker.
The foregoing examples illustrate the application in detail, but are merely preferred embodiments of the application and are not to be construed as limiting the scope of the application. All equivalent changes and modifications within the scope of the present application are intended to be covered by the present application.
Claims (9)
1. A low energy consumption carbon trapping cement clinker production system is characterized in that: the low-energy-consumption carbon-trapping cement clinker production system comprises a cooler, a rotary kiln, a smoke chamber, a decomposing furnace, an A-row cyclone preheater, a B-row cyclone preheater and a C-row cyclone preheater, wherein blanking pipes of the A-row cyclone preheater, the B-row cyclone preheater and the C-row cyclone preheater are connected with a feeding port of the decomposing furnace, an outlet of the decomposing furnace is connected with an air inlet of the A-row lowest-stage cyclone preheater, the blanking pipe of the A-row lowest-stage cyclone preheater is connected with the smoke chamber, the smoke chamber is not directly communicated with the decomposing furnace, the smoke chamber, the rotary kiln and the cooler are sequentially connected, high-temperature air exiting the cooler is divided into three paths, and the first path of air is used as secondary air to directly enter the rotary kiln for fuel combustion, and then enters the B-row cyclone preheater through the air inlet of the B-row lowest-stage cyclone preheater; the second path of air enters the C-column cyclone preheater through the air inlet of the lowest stage cyclone preheater in the C-column; the third air enters a waste heat utilization system, and after the waste heat is utilized, the waste heat is treated by a flue gas treatment system and then discharged into the atmosphere.
2. The low energy carbon capture cement clinker production system of claim 1, wherein: and the discharging pipes of the first-last cyclone preheater in the A column, the second-last cyclone preheater in the B column and the second-last cyclone preheater in the C column are connected with the feeding port of the decomposing furnace.
3. The low energy carbon capture cement clinker production system of claim 1, wherein: the number of the cyclone preheaters in the A column is three to seven, the number of the cyclone preheaters in the B column is three to seven, and the number of the cyclone preheaters in the C column is three to seven.
4. The low energy carbon capture cement clinker production system of claim 1, wherein: the flue gas from the decomposing furnace enters a cyclone preheater A, and the flue gas leaving the cyclone preheater A is divided into two paths, wherein one path of flue gas is high prepared by an air separation deviceMixing the pure oxygen in a certain proportion, and then introducing the mixed gas into the bottom of the decomposing furnace; the other path of flue gas is cooled by a heat exchanger, the cooled flue gas is subjected to flue gas dust removal by a dust remover, and the dust removed flue gas enters CO 2 And (5) capturing and purifying the system.
5. The low energy carbon capture cement clinker production system of claim 4, wherein: o in the mixed gas 2 The volume ratio is 20-80%.
6. The low energy carbon capture cement clinker production system of claim 4, wherein: the air leaving from the outlet of the C-column cyclone preheater is divided into two paths, wherein one path of air enters the waste heat utilization system, the other path of air enters the heat exchanger system through the circulating fan, indirect heat exchange is carried out on the air and the mixed gas in the heat exchanger system, and the air enters the waste heat utilization system after heat exchange is finished.
7. The low energy carbon capture cement clinker production system of claim 1, wherein: the temperature of the first path of air is 950-1200 ℃; the temperature of the second air is 850-1000 ℃; the temperature of the third air is 250-450 ℃.
8. The low energy carbon capture cement clinker production system of claim 1, wherein: the flue gas from the cyclone preheater B enters a waste heat utilization system, and after the waste heat is utilized, the flue gas is treated by a flue gas treatment system and then is discharged into the atmosphere; and the flue gas discharged from the C-column cyclone preheater enters a waste heat utilization system, and is discharged to the atmosphere after being treated by a flue gas treatment system after being utilized by waste heat.
9. A method for preparing cement clinker by low-energy-consumption carbon capture is characterized by comprising the following steps: the method for preparing cement clinker by low-energy carbon capture uses the low-energy carbon capture cement clinker production system according to any one of claims 1 to 8.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103253879A (en) * | 2013-05-07 | 2013-08-21 | 华南理工大学 | Cement clinker production technology for enriching CO2 by use of O2/CO2 combustion technology |
| CN107235647A (en) * | 2017-06-30 | 2017-10-10 | 中国建筑材料科学研究总院 | Oxygen/carbon dioxide combustion technology applied to cement clinker production technology |
| CN210855853U (en) * | 2019-08-12 | 2020-06-26 | 天津水泥工业设计研究院有限公司 | Adjustable CO reformed from off-line decomposer2Enrichment amount cement kiln system |
| CN210922156U (en) * | 2019-08-12 | 2020-07-03 | 天津水泥工业设计研究院有限公司 | Cement predecomposition kiln system |
| CN112321183A (en) * | 2020-11-12 | 2021-02-05 | 天津水泥工业设计研究院有限公司 | Cement kiln system for realizing zero emission of carbon dioxide and cement clinker preparation method |
| CN112390551A (en) * | 2019-08-12 | 2021-02-23 | 天津水泥工业设计研究院有限公司 | Adjustable CO reformed from off-line decomposer2Enrichment cement kiln system and method |
| CN112390553A (en) * | 2019-08-12 | 2021-02-23 | 天津水泥工业设计研究院有限公司 | Can realize CO2Zero-emission cement kiln system and method for preparing cement clinker |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2009245238B2 (en) * | 2008-05-07 | 2014-06-12 | Mitsubishi Materials Corporation | Method and apparatus for recovering CO2 gas in cement production equipment |
-
2022
- 2022-06-29 CN CN202210759027.3A patent/CN115159876B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103253879A (en) * | 2013-05-07 | 2013-08-21 | 华南理工大学 | Cement clinker production technology for enriching CO2 by use of O2/CO2 combustion technology |
| CN107235647A (en) * | 2017-06-30 | 2017-10-10 | 中国建筑材料科学研究总院 | Oxygen/carbon dioxide combustion technology applied to cement clinker production technology |
| CN210855853U (en) * | 2019-08-12 | 2020-06-26 | 天津水泥工业设计研究院有限公司 | Adjustable CO reformed from off-line decomposer2Enrichment amount cement kiln system |
| CN210922156U (en) * | 2019-08-12 | 2020-07-03 | 天津水泥工业设计研究院有限公司 | Cement predecomposition kiln system |
| CN112390551A (en) * | 2019-08-12 | 2021-02-23 | 天津水泥工业设计研究院有限公司 | Adjustable CO reformed from off-line decomposer2Enrichment cement kiln system and method |
| CN112390553A (en) * | 2019-08-12 | 2021-02-23 | 天津水泥工业设计研究院有限公司 | Can realize CO2Zero-emission cement kiln system and method for preparing cement clinker |
| CN112321183A (en) * | 2020-11-12 | 2021-02-05 | 天津水泥工业设计研究院有限公司 | Cement kiln system for realizing zero emission of carbon dioxide and cement clinker preparation method |
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