CN217939696U - Cement industry carbon dioxide enrichment system - Google Patents
Cement industry carbon dioxide enrichment system Download PDFInfo
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- CN217939696U CN217939696U CN202221007918.5U CN202221007918U CN217939696U CN 217939696 U CN217939696 U CN 217939696U CN 202221007918 U CN202221007918 U CN 202221007918U CN 217939696 U CN217939696 U CN 217939696U
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- preheater
- auxiliary
- carbon dioxide
- main
- decomposing furnace
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 57
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 57
- 239000004568 cement Substances 0.000 title claims abstract description 22
- 239000000463 material Substances 0.000 claims abstract description 55
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 35
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 35
- 239000001301 oxygen Substances 0.000 claims abstract description 35
- 239000002994 raw material Substances 0.000 claims abstract description 24
- 239000000779 smoke Substances 0.000 claims abstract description 23
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims abstract description 9
- 239000000428 dust Substances 0.000 claims description 8
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 claims description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 23
- 239000003546 flue gas Substances 0.000 abstract description 23
- 238000000354 decomposition reaction Methods 0.000 abstract description 16
- 230000000694 effects Effects 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 9
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 7
- 238000002485 combustion reaction Methods 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 125000005587 carbonate group Chemical group 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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Abstract
The utility model relates to a carbon dioxide enrichment system in cement industry, which comprises a main preheater, a main decomposition furnace, a smoke chamber, a rotary kiln, a tertiary air pipe, a cooler and a cooling fan, wherein the main preheater, the main decomposition furnace, the smoke chamber, the rotary kiln and the cooler are sequentially connected in series along a material path, and the cooling fan, the cooler, the rotary kiln, the smoke chamber main decomposition furnace and the main preheater are sequentially connected along a gas path; the system also comprises a raw material feeding device, an auxiliary decomposing furnace, an auxiliary preheater, a circulating fan, an oxygen generating device, an oxygen supply fan, a heat exchanger and a carbon dioxide trapping device, wherein the oxygen generating device, the oxygen supply fan, the auxiliary decomposing furnace and the auxiliary preheater are sequentially connected along a gas path; the utility model discloses both realized the entrapment and the utilization cost of carbon dioxide in order to reduce carbon dioxide by a wide margin to the enrichment of part kiln tail flue gas carbon dioxide, effectively reduced again to kiln system negative effects.
Description
Technical Field
The utility model relates to a cement industry carbon dioxide enrichment and emission reduction technical field, concretely relates to cement industry carbon dioxide part enrichment system.
Background
Carbon dioxide emission reduction is a key problem of global attention at present, the government of China actively promotes green low-carbon development, and the promise of striving to realize carbon peak reaching in 2030 years and carbon neutralization in 2060 years means that China can carry out large-scale carbon dioxide emission reduction in a plurality of industrial fields.
In the cement industry, a large amount of carbon dioxide is generated by burning fuel (mainly taking coal as main fuel) and decomposing calcium carbonate serving as a main raw material component in raw materials in the cement production process, certain carbon dioxide emission reduction is realized by saving energy and reducing energy consumption in the cement calcination process, but the carbon dioxide emission reduction proportion is small, and the capture and utilization of the carbon dioxide in flue gas are common technical schemes in the cement industry and are also one of main measures for reducing carbon in the future cement industry.
At present, the cement industry has a technology for capturing and purifying carbon dioxide from kiln tail flue gas by using a chemical absorption method, the technology is used for absorbing and capturing the carbon dioxide in the kiln tail waste gas on the premise of not influencing the normal production of a cement kiln, but the carbon dioxide capturing cost is higher, and the problems of degradation of a chemical absorbent and the like exist.
Carbon dioxide concentration generally is 27-30% in the flue gas of kiln tail preheater export among the existing cement industry, after waste heat power generation cooling, stoving raw materials grind the system, because each system all has certain air leakage, in addition raw materials moisture content turns into the steam in the flue gas, carbon dioxide concentration further reduces before reaching the chimney emission, carbon dioxide volume content generally is 17-22%, lower carbon dioxide concentration leads to follow-up entrapment and use cost higher, can cause great negative effect to kiln system moreover, urgent need to solve.
SUMMERY OF THE UTILITY MODEL
To the current situation of above-mentioned prior art, the utility model aims to solve the technical problem that a cement industry carbon dioxide enrichment system has not only been realized to the enrichment of part kiln tail flue gas carbon dioxide in order to reduce carbon dioxide by a wide margin with the utilization cost, has effectively reduced the negative impact to kiln system again.
The utility model provides a technical scheme that above-mentioned technical problem adopted does: a carbon dioxide enrichment system in the cement industry comprises a main preheater, a main decomposing furnace, a smoke chamber, a rotary kiln, a tertiary air pipe, a cooler and a cooling fan, wherein the main preheater, the main decomposing furnace, the smoke chamber, the rotary kiln and the cooler are sequentially connected in series along a material path; the main preheater comprises a plurality of first cyclone cylinders which are connected in series, and is characterized by further comprising a raw material feeding device, an auxiliary decomposing furnace, an auxiliary preheater, a circulating fan, an oxygen generating device, an oxygen supply fan, a heat exchanger and a carbon dioxide collecting device, wherein the oxygen generating device, the oxygen supply fan, the auxiliary decomposing furnace and the auxiliary preheater are sequentially connected along a gas path, an air inlet of the auxiliary decomposing furnace and an air inlet of the carbon dioxide collecting device are respectively connected in parallel to an air outlet of the auxiliary preheater through the circulating fan and the heat exchanger, the auxiliary preheater comprises a plurality of second cyclone cylinders which are connected in series, an air inlet pipe of the uppermost second cyclone cylinder in the auxiliary preheater and an air inlet pipe of the uppermost first cyclone cylinder in the main preheater are both connected in parallel to a discharge port of the raw material feeding device, and a discharge pipe of the lowermost second cyclone cylinder in the auxiliary preheater is connected with the main decomposing furnace and a smoke chamber.
Preferably, a dust collector and an induced draft fan are sequentially arranged between the heat exchanger and the air inlet of the carbon dioxide capture device, a first air valve is further arranged on the upstream side of the air inlet of the circulating fan, and a second air valve is further arranged on the upstream side of the air inlet of the heat exchanger.
Preferably, a cold air valve is further arranged between the auxiliary decomposing furnace and the oxygen supply fan, and a third air valve is further arranged between the oxygen supply fan and the cold air valve.
Preferably, a first material valve is further arranged between the discharge pipe of the second lowest-stage cyclone in the auxiliary preheater and the feed inlet of the main decomposing furnace, and a second material valve is further arranged between the discharge pipe of the second lowest-stage cyclone in the auxiliary preheater and the feed inlet of the smoke chamber.
Preferably, a third material valve is arranged between the raw material feeding device and the air inlet pipe of the first cyclone cylinder at the uppermost stage in the main preheater, and a fourth material valve is arranged between the raw material feeding device and the air inlet pipe of the second cyclone cylinder at the uppermost stage in the auxiliary preheater.
Compared with the prior art, the beneficial effects of the utility model are as follows:
1. an auxiliary preheater frame is arranged beside the main preheater and the main decomposing furnace, the auxiliary preheater and the auxiliary decomposing furnace are arranged, reasonable raw material quantity is fed into the auxiliary preheater according to the requirements of carbon dioxide concentration and air quantity, the auxiliary preheater system and the main preheater system are separated to realize material heating and carbonate decomposition, and mutual interference is less.
2. The material after the decomposition of the auxiliary decomposing furnace is arranged into one path to enter the main decomposing furnace, so that the secondary decomposition of carbonate in the material can be realized, the higher decomposition rate of hot raw materials entering the kiln is ensured, and the negative influence on the kiln system is reduced.
3. The utility model carries out carbon dioxide enrichment in the auxiliary preheater and the auxiliary decomposing furnace, and has small trapping difficulty and low cost; and the high-concentration flue gas does not enter the rotary kiln, so that the influence on the calcination in the rotary kiln is small, the method is not different from the conventional ordinary rotary kiln, and the technical risk is reduced.
Drawings
Fig. 1 is a process flow chart of the present invention.
Fig. 2 is a process flow chart of the present invention after a dust collector, a second circulating fan, a first air valve and a second air valve are added.
Fig. 3 is the process flow chart of the utility model after the cold air valve and the air valve are added.
Fig. 4 is a process flow chart of the present invention after adding a material valve i and a material valve ii.
Fig. 5 is a process flow chart of the present invention after adding the third material valve and the fourth material valve.
Wherein: 1. raw material feeding device, 2, main preheater, 3, main decomposing furnace, 4, smoke chamber, 5, rotary kiln, 6, tertiary air pipe, 7, cooler, 8, cooling fan, 9, auxiliary decomposing furnace, 10, auxiliary preheater, 11, first circulating fan, 12, oxygen generator, 13, oxygen supply fan, 14, heat exchanger, 15, dust collector, 16, second circulating fan, 17, fan, 18, cold air valve, 19, material valve I, 20, material valve II, 21, material valve III, 22, material valve IV, 23, air valve I, 24, air valve II, 25 and air valve III.
Detailed Description
Unless defined otherwise, technical or scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The use of the terms "comprising" or "including" and similar referents in the context of describing the invention as being "comprising" and the like, is to be construed to cover the listed referents or items, including but not limited to the listed referents or items, and equivalents thereof. The terms "connected" or "connected" and the like are not limited to physical or mechanical connections, and "upper" and "lower" are used merely to indicate relative positional relationships, and when the absolute position of a described object is changed, the relative positional relationships may be changed accordingly.
To keep the following description of the embodiments of the present invention clear and concise, a detailed description of known functions and known parts of the invention has been omitted.
As shown in fig. 1, a carbon dioxide enrichment system in cement industry comprises a main preheater 2, a main decomposing furnace 3, a smoke chamber 4, a rotary kiln 5, a tertiary air pipe 6, a cooler 7 and a cooling fan 8, wherein the main preheater 2, the main decomposing furnace 3, the smoke chamber 4, the rotary kiln 5 and the cooler 7 are sequentially connected in series along a material path, the main decomposing furnace 3 is mutually communicated with the cooler 7 through the tertiary air pipe 6, and the cooling fan 8, the cooler 7, the rotary kiln 5, the smoke chamber 4, the main decomposing furnace 3 and the main preheater 2 are sequentially connected along a gas path; the main preheater 2 comprises a plurality of first cyclones 2-1 which are connected in series, and also comprises a raw material feeding device 1, an auxiliary decomposing furnace 9, an auxiliary preheater 10, a circulating fan 11, an oxygen generating device 12, an oxygen supply fan 13, a heat exchanger 14 and a carbon dioxide trapping device 17, wherein the oxygen generating device 12, the oxygen supply fan 13, the auxiliary decomposing furnace 9 and the auxiliary preheater 10 are sequentially connected along a gas path, and an air inlet of the auxiliary decomposing furnace 9 and an air inlet of the carbon dioxide trapping device 17 are respectively connected in parallel on an air outlet of the auxiliary preheater 10 through the circulating fan 11 and the heat exchanger 14; the auxiliary preheater 10 comprises a plurality of second cyclones 10-1 which are connected in series, and the air inlet pipe of the uppermost second cyclone 10-1 in the auxiliary preheater 10 and the air inlet pipe of the uppermost first cyclone 2-1 in the main preheater 2 are connected in parallel on the discharge hole of the raw material feeding device 1; a discharge pipe of the second cyclone cylinder 10-1 at the lowest stage in the auxiliary preheater 10 is connected with the main decomposing furnace 3 and the smoke chamber 4; the heat exchanger 14 can reduce the temperature of the high-temperature flue gas (generally above 300 ℃) discharged from the air outlet of the auxiliary preheater 10 to provide conditions for subsequent carbon dioxide capture.
In order to improve the functions of the utility model, a dust collector 15 and a draught fan 16 are sequentially arranged between the heat exchanger 14 and the air inlet of the carbon dioxide collecting device 17, and the dust collector 15 can remove dust from the cooled flue gas discharged from the heat exchanger 14; in order to adjust the air volume ratio from the flue gas of the auxiliary preheater 10 to the auxiliary decomposing furnace 9 and the carbon dioxide trapping device 17, the upstream side of the air inlet of the circulating fan 11 is further provided with a first air valve 23, the upstream side of the air inlet of the heat exchanger 14 is further provided with a second air valve 24, the adjustment of the trapped flue gas volume and the control of the circulating air volume can be realized by adjusting the opening degrees of the first air valve 23 and the second air valve 24, and the adjustment and the control of the carbon dioxide concentration of the flue gas generated in the auxiliary decomposing furnace 9 are facilitated, as shown in fig. 2.
In order to further improve the functions of the utility model, a cold air valve 18 is arranged between the auxiliary decomposing furnace 9 and the oxygen supply fan 13, a third air valve 25 is arranged between the oxygen supply fan 13 and the cold air valve 18, and normal air combustion in the auxiliary decomposing furnace 9 and adjustment of air volume and carbon dioxide concentration can be realized by adjusting the opening degrees of the cold air valve 18 and the third air valve 25; when the oxygen supply of the oxygen generating device 13 is stopped, the third air valve 25 is closed and the cold air valve 18 is opened, so that normal air oxygen supply combustion can be realized; when the oxygen generator 13 starts to supply oxygen, the cold air valve 18 is closed and the third air valve 25 is opened, so that oxygen enrichment or pure oxygen can be supplied to the auxiliary decomposing furnace 9 for fuel combustion, and high-concentration carbon dioxide flue gas is generated; the cold air valve 18 and the air valve III 25 can also be opened simultaneously, and the flue gas amount and the carbon dioxide concentration of the auxiliary decomposing furnace 9 can be controlled by adjusting the opening degree, as shown in FIG. 3.
In order to further optimize the functions of the utility model, a first material valve 19 is arranged between the discharging pipe of the second cyclone 10-1 at the lowest stage in the auxiliary preheater 10 and the feeding hole of the main decomposing furnace 3, a second material valve 20 is arranged between the discharging pipe of the second cyclone 10-1 at the lowest stage in the auxiliary preheater 10 and the feeding hole of the smoke chamber 4, and the material decomposed by the auxiliary decomposing furnace 9 can enter the main decomposing furnace 3 to firstly carry out secondary decomposition of carbonate through the switching of the first material valve 19 and the second material valve 20, and then enters the rotary kiln 5 through the smoke chamber 4, or directly enters the rotary kiln 5 through the smoke chamber 4; when the concentration of carbon dioxide in the auxiliary decomposing furnace 9 is higher, the decomposition rate of carbonate in the furnace is possibly reduced, at the moment, the first material valve 19 can be opened and the second material valve 20 can be closed so as to feed the materials in the auxiliary decomposing furnace 9 into the main decomposing furnace 3 through the lowest stage cyclone 10-1 in the auxiliary preheater 10, so that the secondary decomposition of the carbonate in the materials is realized, and the materials are converged together with the materials in the main decomposing furnace 3 and then enter the rotary kiln 5 to be calcined into clinker; if the decomposition rate of the carbonate in the auxiliary decomposing furnace 9 is always over 93 percent, the first material valve 19 can be closed and the second material valve 20 can be opened so as to directly feed the decomposed materials into the rotary kiln 5 through the smoke chamber 4, and the materials and the decomposed materials of the carbonate in the main decomposing furnace 3 are calcined in the rotary kiln 5 together, as shown in figure 4.
In order to further realize the accurate operation of the utility model, a third material valve 21 is arranged between the raw material feeding device 1 and the air inlet pipe of the uppermost first cyclone 2-1 in the main preheater 2, a fourth material valve 22 is arranged between the raw material feeding device 1 and the air inlet pipe of the uppermost second cyclone 10-1 in the auxiliary preheater 10, and the material amount fed into the main preheater 2 and the auxiliary preheater 10 is adjusted by controlling the opening and closing of the third material valve 21 and the fourth material valve 22; the third material valve 21 and the fourth material valve 22 can realize the functions of material distribution and cut-off, and can realize the matching of the material and the gas quantity according to the concentration requirement of the carbon dioxide and the gas quantity of the auxiliary decomposing furnace 3 and the auxiliary preheater 2, as shown in fig. 5.
The process principle is as follows:
s1: the cement raw material is divided into two paths by a raw material feeding device 1, one path of the raw material is fed into a main preheater 2, exchanges heat with the flue gas from a main decomposing furnace 3, and then enters the main decomposing furnace 3 for carbonate decomposition; the other path is fed into an auxiliary preheater 10, exchanges heat with the flue gas from the auxiliary decomposing furnace 9, and then enters the auxiliary decomposing furnace 9 for carbonate decomposition.
S2: when the decomposition rate of the carbonate is high, the decomposed materials can directly enter a rotary kiln 5 through a smoke chamber 4 to be calcined; when the decomposition rate is low, the material can enter the main decomposing furnace 3 for secondary decomposition, and then enter the rotary kiln 5 through the smoke chamber 4 to be calcined into clinker.
S3: the amount of raw materials entering the main preheater 2 and the auxiliary preheater 10 is regulated and controlled by a third material valve 21 and a fourth material valve 22; the switching of the material decomposed by the auxiliary decomposing furnace 3 into the main decomposing furnace 3 and the smoke inlet chamber 4 is realized through the on-off control of the first material valve 19 and the second material valve 20.
S4: the flue gas out of the auxiliary preheater 10 is divided into two paths, one path circulates part of the flue gas to the auxiliary decomposing furnace 9 through the circulating fan 11, so that the enrichment of carbon dioxide in the flue gas in the auxiliary preheater 10 is realized, and the concentration of the carbon dioxide in the flue gas is further improved; the other path of the flue gas is communicated with a carbon dioxide trapping device 17, a heat exchanger 14 and a dust collector 15 are arranged between an air outlet pipe of the auxiliary preheater 10 and the carbon dioxide trapping device 17, so that the high-temperature flue gas (generally above 300 ℃) at the outlet of the auxiliary preheater 10 can be cooled and dedusted, and conditions are provided for trapping the carbon dioxide; the flue gas volume of the auxiliary preheater 10 to the two paths is adjusted through a first valve 23 and a second air valve 24.
S5: pure oxygen or rich oxygen is introduced into the auxiliary decomposing furnace 9 through the oxygen generating device 12 and the oxygen supply fan 13 so as to make up for the negative influence in the environment of high-concentration carbon dioxide in the auxiliary decomposing furnace 9 and contribute to the combustion of fuel in the auxiliary decomposing furnace 9; the air pipe between the auxiliary decomposing furnace 9 and the oxygen supply fan 13 is provided with the cold air valve 18, the air pipe between the oxygen supply fan 13 and the cold air valve 18 is provided with the third air valve 25, normal air combustion in the auxiliary decomposing furnace 9 can be realized through adjustment of the two air valves, and the air volume and carbon dioxide concentration can also be adjusted.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that the technical solutions described in the foregoing embodiments may be modified or some technical features may be equally replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention in its corresponding aspects.
Claims (5)
1. A carbon dioxide enrichment system in the cement industry comprises a main preheater (2), a main decomposing furnace (3), a smoke chamber (4), a rotary kiln (5), a tertiary air pipe (6), a cooler (7) and a cooling fan (8), wherein the main preheater (2), the main decomposing furnace (3), the smoke chamber (4), the rotary kiln (5) and the cooler (7) are sequentially connected in series along a material path, the main decomposing furnace (3) is communicated with the cooler (7) through the tertiary air pipe (6), and the cooling fan (8), the cooler (7), the rotary kiln (5), the smoke chamber (4), the main decomposing furnace (3) and the main preheater (2) are sequentially connected along a gas path; the main preheater (2) comprises a plurality of first cyclones (2-1) which are connected in series, and is characterized by further comprising a raw material feeding device (1), an auxiliary decomposing furnace (9), an auxiliary preheater (10), a circulating fan (11), an oxygen generating device (12), an oxygen supply fan (13), a heat exchanger (14) and a carbon dioxide trapping device (17), wherein the oxygen generating device (12), the oxygen supply fan (13), the auxiliary decomposing furnace (9) and the auxiliary preheater (10) are sequentially connected along a gas path, and an air inlet of the auxiliary decomposing furnace (9) and an air inlet of the carbon dioxide trapping device (17) are respectively connected in parallel to an air outlet of the auxiliary preheater (10) through the circulating fan (11) and the heat exchanger (14); the auxiliary preheater (10) comprises a plurality of second cyclones (10-1) which are connected in series, and an air inlet pipe of the uppermost second cyclone (10-1) in the auxiliary preheater (10) and an air inlet pipe of the uppermost first cyclone (2-1) in the main preheater (2) are connected in parallel to a discharge hole of the raw material feeding device (1); the discharge pipe of the second cyclone cylinder (10-1) at the lowest stage in the auxiliary preheater (10) is connected with the main decomposing furnace (3) and the smoke chamber (4).
2. The carbon dioxide enrichment system for the cement industry according to claim 1, characterized in that a dust collector (15) and an induced draft fan (16) are further sequentially arranged between the heat exchanger (14) and the air inlet of the carbon dioxide capture device (17), a first air valve (23) is further arranged on the upstream side of the air inlet of the circulating fan (11), and a second air valve (24) is further arranged on the upstream side of the air inlet of the heat exchanger (14).
3. The carbon dioxide enrichment system for the cement industry as claimed in claim 2, characterized in that a cold air valve (18) is further arranged between the auxiliary decomposing furnace (9) and the oxygen supply fan (13), and a third air valve (25) is further arranged between the oxygen supply fan (13) and the cold air valve (18).
4. A cement industry carbon dioxide enrichment system according to claim 3, characterized in that a first material valve (19) is further provided between the discharge pipe of the second cyclone (10-1) at the lowest stage in the secondary preheater (10) and the feed inlet of the main decomposing furnace (3), and a second material valve (20) is further provided between the discharge pipe of the second cyclone (10-1) at the lowest stage in the secondary preheater (10) and the feed inlet of the flue chamber (4).
5. A carbon dioxide enrichment system in cement industry according to claim 4 characterized in that a third material valve (21) is arranged between the raw material feeding device (1) and the air inlet pipe of the first cyclone (2-1) in the uppermost stage of the primary preheater (2), and a fourth material valve (22) is arranged between the raw material feeding device (1) and the air inlet pipe of the second cyclone (10-1) in the uppermost stage of the secondary preheater (10).
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| CN202221007918.5U CN217939696U (en) | 2022-04-27 | 2022-04-27 | Cement industry carbon dioxide enrichment system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114739163A (en) * | 2022-04-27 | 2022-07-12 | 南京凯盛国际工程有限公司 | Carbon dioxide enrichment system for cement industry and process principle thereof |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114739163A (en) * | 2022-04-27 | 2022-07-12 | 南京凯盛国际工程有限公司 | Carbon dioxide enrichment system for cement industry and process principle thereof |
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Address after: 303 Hanzhongmen street, Gulou District, Nanjing City, Jiangsu Province Patentee after: Zhongcai International Intelligent Technology Co.,Ltd. Patentee after: China Building Materials Group Co.,Ltd. Address before: 303 Hanzhongmen street, Gulou District, Nanjing City, Jiangsu Province Patentee before: NANJING KISEN INTERNATIONAL ENGINEERING Co.,Ltd. Patentee before: China Building Materials Group Co.,Ltd. |
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