CN112393597A - Cement firing system and method based on pure oxygen combustion - Google Patents
Cement firing system and method based on pure oxygen combustion Download PDFInfo
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- CN112393597A CN112393597A CN201910739793.1A CN201910739793A CN112393597A CN 112393597 A CN112393597 A CN 112393597A CN 201910739793 A CN201910739793 A CN 201910739793A CN 112393597 A CN112393597 A CN 112393597A
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- oxygen
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- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 61
- 239000004568 cement Substances 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000010304 firing Methods 0.000 title claims abstract description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 63
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 63
- 239000001301 oxygen Substances 0.000 claims abstract description 63
- 239000007789 gas Substances 0.000 claims abstract description 45
- 238000001816 cooling Methods 0.000 claims abstract description 44
- 239000003546 flue gas Substances 0.000 claims abstract description 35
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000002918 waste heat Substances 0.000 claims abstract description 31
- 238000002360 preparation method Methods 0.000 claims abstract description 25
- 238000011084 recovery Methods 0.000 claims abstract description 14
- 239000000446 fuel Substances 0.000 claims description 13
- 239000002994 raw material Substances 0.000 claims description 12
- 238000006477 desulfuration reaction Methods 0.000 claims description 9
- 230000023556 desulfurization Effects 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 9
- 238000001179 sorption measurement Methods 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 8
- 238000001354 calcination Methods 0.000 claims description 4
- 239000011819 refractory material Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 4
- 235000012054 meals Nutrition 0.000 claims description 3
- 238000005266 casting Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 238000011278 co-treatment Methods 0.000 claims 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 claims 1
- 239000000779 smoke Substances 0.000 abstract description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract 1
- 238000005245 sintering Methods 0.000 abstract 1
- 239000003245 coal Substances 0.000 description 7
- 238000007599 discharging Methods 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B19/00—Combinations of furnaces of kinds not covered by a single preceding main group
- F27B19/04—Combinations of furnaces of kinds not covered by a single preceding main group arranged for associated working
-
- 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
-
- 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
- C04B7/47—Cooling ; Waste heat management
- C04B7/475—Cooling ; Waste heat management using the waste heat, e.g. of the cooled clinker, in an other way than by simple heat exchange in the cement production line, e.g. for generating steam
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
- F23L7/007—Supplying oxygen or oxygen-enriched air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D13/00—Apparatus for preheating charges; Arrangements for preheating charges
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D15/00—Handling or treating discharged material; Supports or receiving chambers therefor
- F27D15/02—Cooling
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
- Y02P40/18—Carbon capture and storage [CCS]
Abstract
The invention provides a cement firing system and method based on pure oxygen combustion, wherein the system comprises a pure oxygen preparation device, an oxygen delivery pipe, a rotary kiln, a tertiary air pipe, a decomposing furnace, a kiln tail preheater, a high-temperature fan, a tail gas treatment device, a CO (carbon monoxide) treatment device2Catching equipment, cooler, blower, cooler hot air pipe, cooler residual air pipe and residual heat recovery deviceAnd a heat exchanger; the method comprises the steps of carrying out heat exchange on oxygen produced by a pure oxygen preparation device and high-temperature waste heat produced by a cooling machine to produce high-temperature pure oxygen; dividing the generated high-temperature pure oxygen into three paths, and respectively conveying the three paths of high-temperature pure oxygen to a decomposing furnace, a rotary kiln and a kiln head burner; the flue gas generated by combustion is treated by a tail gas treatment device and CO is carried out2Trapping; and introducing the clinker calcined in the rotary kiln into the cooling machine for cooling, and recovering waste heat. The invention can effectively improve the combustion efficiency, improve the combustion temperature and reduce the smoke gas amount, thereby reducing the heat consumption of cement sintering.
Description
Technical Field
The invention belongs to the field of cement preparation, and particularly relates to a cement firing system and method based on pure oxygen combustion.
Background
The cement is a powdery hydraulic inorganic cementing material; water is added and stirred to form slurry which can be hardened in the air or in water, and sand, stone and other materials can be firmly cemented together, and the slurry is generally used in the construction industry; during production of cement, various materials such as limestone, clay, iron ore and coal are mostly crushed and fired.
The existing cement burning system adopts the mode of blowing air during burning to provide the oxygen required by burning, the burning mode has low burning efficiency, simultaneously, in order to meet the burning requirement, a large amount of air needs to be blown, the relative energy consumption is large, and the huge flue gas volume can also increase the burden of a series of process flows such as flue gas dust removal, desulfurization, denitration and the like.
Disclosure of Invention
In order to solve the problems, the invention provides a cement burning system and a method based on pure oxygen combustion.
A cement burning system based on pure oxygen combustion comprises,
a pure oxygen preparation device for producing oxygen;
the oxygen conveying pipe is connected with the pure oxygen preparation device;
the rotary kiln is connected with the oxygen conveying pipe, and the oxygen conveying pipe is used for conveying high-temperature pure oxygen into the rotary kiln; the end part of the rotary kiln is connected with a kiln head burner, the kiln head burner is connected with the oxygen conveying pipe, and the oxygen conveying pipe is used for conveying high-temperature pure oxygen into the kiln head burner;
the tertiary air pipe is communicated with the oxygen conveying pipe;
the decomposing furnace is connected with the tertiary air pipe, and the tertiary air pipe is used for conveying high-temperature pure oxygen into the decomposing furnace to supply fuel for combustion; the decomposing furnace is also connected with the rotary kiln, and the rotary kiln is used for calcining the hot raw meal discharged from the decomposing furnace;
the kiln tail preheater is connected with the decomposing furnace and is used for preheating raw materials;
the high-temperature fan is connected with the kiln tail preheater through a pipeline and used for carrying out traction conveying on flue gas generated after combustion;
the tail gas treatment device is connected with the high-temperature fan and is used for carrying out dust removal, desulfurization and denitration treatment on the conveyed flue gas;
a CO2 capturing device, wherein the CO2 capturing device is connected with the tail gas processing device, and the CO2 capturing device is used for capturing CO2 of the processed flue gas;
the cooler is connected with the rotary kiln and is used for cooling clinker output by the rotary kiln;
a blower provided at a side of the cooler, the blower for providing sufficient cooling wind into the cooler;
one end of the cooler hot air pipe is connected with the cooler, and the cooler hot air pipe is used for conveying hot air generated by the front half section of the cooler;
one end of the cooler exhaust pipe is connected with the cooler, and the cooler exhaust pipe is used for conveying hot air generated by the rear half section of the cooler; the cooler hot air pipe and the cooler residual air pipe are arranged at the top of the cooler;
the waste heat recovery device is connected with the tail ends of the hot air pipe of the cooler and the waste air pipe of the cooler and is used for recovering waste heat of the conveyed hot air;
the heat exchanger is connected with the oxygen conveying pipe and the hot air pipe of the cooling machine and used for carrying out heat exchange on pure oxygen and high-temperature waste heat air and preheating the pure oxygen into the high-temperature pure oxygen.
Further, the pure oxygen preparation device adopts a low-temperature air separation or pressure swing adsorption mode to produce high-concentration oxygen-containing gas, wherein the oxygen content in the oxygen-containing gas is 95% or more.
Further, the kiln tail preheater comprises a multi-stage arrangement cyclone cylinder, and the stage number of the multi-stage arrangement cyclone cylinder comprises four stages, five stages or six stages.
Furthermore, the rotary kiln is connected with the cooling machine through a feeding necking, and the feeding necking is funnel-shaped.
Further, the temperature of air in the hot air pipe of the cooler is 950-1000 ℃, and the air volume is 0.6-0.7 Nm 3/kg.cl; the amount of the high-temperature pure oxygen is 0.2-0.25 Nm3/kg. cl, and the temperature is 760-800 ℃ after the heat exchange with the hot air is completed.
Furthermore, air quantity control valves are arranged at the joint of the oxygen conveying pipe and the tertiary air pipe, the joint of the oxygen conveying pipe and the kiln head burner and the joint of the oxygen conveying pipe and the rotary kiln.
Furthermore, the pouring material in the decomposing furnace is made of a high-temperature refractory material which can resist more than 1500 ℃.
A cement firing method based on pure oxygen combustion comprises the following steps,
carrying out heat exchange on oxygen produced by the pure oxygen preparation device and high-temperature waste heat produced by a cooling machine through a heat exchanger to generate high-temperature pure oxygen;
dividing the generated high-temperature pure oxygen into three paths, and respectively conveying the three paths of high-temperature pure oxygen to a decomposing furnace filled with raw materials, a rotary kiln and a kiln head combustor for combustion;
treating flue gas generated by combustion through a tail gas treatment device, and capturing CO2 in the flue gas through a CO2 capturing device;
and (3) introducing the clinker calcined in the rotary kiln into the cooling machine for cooling, and recovering waste heat through a waste heat recovery device.
Further, the step of processing the flue gas generated by combustion through a tail gas processing device and capturing CO2 in the flue gas through a CO2 capturing device comprises the steps of,
after the tail gas is subjected to dust removal, desulfurization and denitration processes, CO2 gas with the concentration of more than 80% is obtained;
the obtained CO2 gas is treated by an adsorption rectification mode to obtain CO2 gas with the purity of more than 99%.
The invention adopts a heat exchange mode to heat the pure oxygen participating in the combustion, improves the combustion efficiency, and simultaneously divides the generated high-temperature pure oxygen into three paths to enter a combustion system, improves the combustion temperature, reduces the smoke gas amount, thereby reducing the heat consumption of cement combustion.
Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and claims hereof as well as the appended drawings.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and those skilled in the art can also obtain other drawings according to the drawings without creative efforts.
FIG. 1 shows a schematic view of a cement firing system according to an embodiment of the invention;
FIG. 2 shows a schematic structural diagram of a chiller according to an embodiment of the present invention;
FIG. 3 shows a schematic structural view of a kiln head burner according to an embodiment of the invention;
FIG. 4 shows a schematic flow diagram of a cement firing method according to an embodiment of the invention.
Shown in the figure: 1. pure oxygen preparation device, 2, heat exchanger, 3, oxygen conveying pipe, 4, cooler hot air pipe, 5, cooler exhaust air pipe, 6, exhaust heat recovery device, 7, blower, 8, cooler, 81, cooler air chamber, 9, rotary kiln, 91, kiln head burner, 911, cooling air duct, 912, axial flow air duct, 913, coal feeding air duct, 914, rotational flow air duct, 92, kiln door cover, 93, blanking necking, 10, decomposing furnace, 11, kiln tail preheater, 12, tertiary air duct, 13, tail gas treatment device, 14, high temperature fan, 15, CO2A trapping device.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The present invention provides a cement burning system based on pure oxygen combustion, exemplarily, as shown in fig. 1, the cement burning system comprises,
a pure oxygen preparation device 1, wherein the pure oxygen preparation device 1 adopts a low-temperature air separation or pressure swing adsorption mode to produce oxygen-containing gas, and the oxygen content in the oxygen-containing gas is 95% or more; the output end of the pure oxygen preparation device 1 is connected with an oxygen conveying pipe 3, and the oxygen conveying pipe 3 is used for conveying the pure oxygen prepared by the pure oxygen preparation device 1; the output end of the oxygen conveying pipe 3 is connected with the tertiary air pipe 12, the tertiary air pipe 12 is connected with the decomposing furnace 10, and the tertiary air pipe 12 conveys the produced pure oxygen into the decomposing furnace 10 for fuel combustion in the decomposing furnace 10 to provide heat for decomposition of raw materials; the decomposing furnace 10 is connected with the rotary kiln 9, and the rotary kiln 9 is used for calcining the thermal raw meal decomposed by the decomposing furnace 10; the rotary kiln 9 is connected with the oxygen conveying pipe 3, a kiln door cover 92 is arranged on the discharging side of the rotary kiln 9, the oxygen conveying pipe 3 is connected with the rotary kiln 9 through the kiln door cover 92, and the conveying pipe 3 conveys pure oxygen into the rotary kiln 9. A kiln head burner 91 is arranged at the discharge port of the rotary kiln 9, and the kiln head burner 91 is connected with the oxygen conveying pipe 3 and supplies oxygen required for forming the flame shape to the kiln head burner 91; the top end of the decomposing furnace 10 is connected with a kiln tail preheater 11, illustratively, the kiln tail preheater 11 adopts a multi-stage series cyclone preheater, and the kiln tail preheater 11 comprises four-stage or five-stage or six-stage cyclone cylinders which are arranged in series; compared with the preheater adopted by the conventional cement production line, the kiln tail preheater 11 configured by pure oxygen combustion has the advantages that the used specification is reduced by 40 percent, and the total smoke gas generated after the oxygen-enriched combustion is adopted is greatly reduced; meanwhile, the specification of the kiln tail preheater 11 is reduced, more smoke heat can be recovered, and the firing heat consumption of the system is reduced.
Kiln tail preheater 11 realizes preheating the raw material that production cement needs, and kiln tail preheater 11 preheats the heat that uses and comes from the high temperature flue gas that dore furnace 10 and rotary kiln 9 burning produced, just kiln tail preheater 11 connects high temperature fan 14, draws the transport through the flue gas after high temperature fan 14 will the heat exchange, and high temperature fan 14 passes through pipe connection tail gas processing apparatus 13, realizes through tail gas processing apparatus 13 that flue gas after the realization is to the flue gasPerforming dust removal, desulfurization, denitration and other processes, and a tail gas treatment device 13 and CO2The trap 15 is connected to pass CO2The trapping device 15 realizes the trapping of CO in the treated flue gas2(ii) a For example, the tail gas treatment device 13 treats the flue gas finally discharged from the firing system through processes of dust removal, desulfurization, denitration and the like, so that the treated CO2The concentration is more than 80 percent to form high-purity flue gas, and then the high-purity flue gas is directly subjected to adsorption rectification to obtain CO with higher purity2Gas (concentration over 99%) and high-purity CO2The gas can be provided for other industrial fields.
The output end of the rotary kiln 9 is connected with a cooler 8, the cooler 8 is used for cooling clinker output by the rotary kiln 9, and two sides of the cooler 8 are provided with blowers 7; the top end of the cooler 8 is connected with a cooler hot air pipe 4 and a cooler residual air pipe 5, and the cooler hot air pipe 4 and the cooler residual air pipe 5 are used for conveying hot air exhausted by the cooler 8; meanwhile, the hot air pipe 4 of the cooler indirectly exchanges heat with the oxygen conveying pipe 3 through the heat exchanger 2, the heat exchange between the high-temperature air and the pure oxygen generated by the pure oxygen preparation device 1 is realized through the heat exchanger 2, the pure oxygen is heated to form high-temperature pure oxygen, and the combustion efficiency can be improved; in order to realize the recovery of the waste heat of the cooler 8 and the reasonable utilization of resources, the cooler hot air pipe 4 connected with the cooler 8 and the cooler waste air pipe 5 are connected with the waste heat recovery device 6, and the waste heat recovery device 6 is used for recovering the waste heat of the high-temperature air generated by the cooler 8.
The generated pure oxygen is subjected to heat exchange with high-temperature air of a cooler 8 through a heat exchanger 2, so that the utilization of high-temperature waste heat is realized, and meanwhile, the combustion temperature and efficiency are improved; the high-temperature air is high-temperature hot air discharged after the clinker is cooled at the front half section of the cooler 8, the temperature of the high-temperature hot air is 950-1000 ℃, and the air volume is 0.6-0.7 Nm3/kg.cl(Nm3The volume of gas at 0 ℃ under 1 standard atmospheric pressure, kg.cl represents kilogram clinker), about 1/3 of the total cooling air volume of the cooling machine 8, and the total oxygen air volume produced by the pure oxygen preparation device 1 is 0.2-0.25 Nm3Cl, temperature of oxygen after heat exchangeThe temperature can reach 760-800 ℃; the oxygen after heat exchange is divided into three paths to enter a burning system, one path replaces secondary air, and directly enters the rotary kiln 9 through the kiln door cover 92, so that fuel burning in the rotary kiln 9 is met. One path of the air replaces tertiary air to enter the decomposing furnace 10, and combustion supporting is provided for combustion in the decomposing furnace 10. And the other path enters a kiln head burner 91 to be used as primary air to provide impulse for flame formed by combustion in the rotary kiln 9. Flue gas generated by combustion of the rotary kiln 9 enters the decomposing furnace 10 and is in contact with CO generated in the decomposing furnace 102The mixed raw materials enter a kiln tail preheater 11 to preheat the raw materials entering a decomposing furnace 10; the flue gas finally discharged from the firing system enters CO through a flue gas treatment device 132A capture system 15 in CO2The CO is obtained after the processes of dust removal, desulfurization, denitration and the like are carried out again in the trapping system 152The high-purity flue gas with the concentration of more than 80 percent can be directly subjected to adsorption rectification to obtain CO with higher purity (more than 99 percent)2Gas, higher purity (over 99%) CO2The gas can be provided for other industrial fields.
FIG. 2 shows a schematic construction of a cooling machine; as shown in fig. 2, one or more cooling blower chambers 81 are provided at the bottom end of the cooling blower 8, and blowers 7 are provided at both sides of the cooling blower chamber 81, and the blowers 7 are used for providing sufficient cooling air for the cooling blower 8; meanwhile, the cooler 8 is connected with the rotary kiln 9 through a blanking necking 93; the cooling air of the cooler 8 is provided by the blower 7, the oxygen-containing air of the rotary kiln 9 is provided by the pure oxygen preparation device 1, the air of the pure oxygen preparation device and the air of the pure oxygen preparation device are separated and do not interfere with each other, clinker discharged from the kiln falls into the cooler 8 through a discharging reducing port 93 for cooling, the discharging reducing port 93 can ensure that the clinker enters the cooler 8 from the rotary kiln 9, and the air blown into the cooler 8 cannot enter the rotary kiln 9. The cooling air blown into the cooler 8 is divided into two pipelines (the hot air pipe 4 of the cooler and the residual air pipe 5 of the cooler) after heat exchange with the clinker, but is not limited to two pipelines leaving the cooler 8. Wherein the cooling air of the hot air pipe 4 of the high temperature section cooler enters the heat exchanger 2 to exchange heat with the pure oxygen. And cooling air of the cooler residual air pipe 5 at the low temperature section and cooling air at the high temperature section after heat exchange are converged and enter the residual heat recovery device 6.
Fig. 3 shows a schematic structural view of the kiln head burner, and as shown in fig. 3, in order to satisfy pure oxygen combustion in the rotary kiln 9, a suitable kiln head burner 91 needs to be separately designed. The burner is used for combustion by pure oxygen, so that the combustion speed of fuel is greatly accelerated, and on the other hand, because the total combustion-supporting gas quantity is greatly reduced and the wind speed in the rotary kiln 9 is greatly reduced, the impulse of the burner is required to be utilized to form flame with enough length, thereby avoiding ultra-high-temperature ultrashort flame formed by too fast combustion of fuel; the kiln head burner 91 used in the present invention has the following structure:
the kiln head burner 91 comprises a cooling air duct 911, an axial flow air duct 912, a coal feeding air duct 913 and a rotational flow air duct 914 from outside to inside. When in use, the large primary air quantity (the primary air is pure oxygen in the oxygen conveying pipeline 3) is adopted, and the sufficient flame length and strength are formed by utilizing the primary air impulse of the kiln head burner 91. The outer shape of the kiln head burner 91 is a circular ring structure, and the air ducts are nested layer by layer from outside to inside. The cooling air channel 911 is arranged on the outermost side, and the cooling air wraps the whole flame, so that the contact between pure oxygen and fuel is slowed down, and the ignition of the fuel is controlled. The axial flow duct 912 is of a porous structure and controls the speed of pure oxygen entering the combustion core region, thereby controlling the combustion speed of the fuel, forming flame with sufficient length, and a low pressure roots blower is used for air supply, wherein the low pressure roots blower is the main source of flame length and impulse. The fuel inlet coal feed air duct 913 is of the same design as the coal feed air duct of a conventional burner head. The swirl air duct 914 is arranged at a small angle of 20-30 degrees, so that a certain effect is achieved on scattering of fuel, and the burnout rate of the fuel can be improved. In addition, in order to improve the combustion efficiency, the characteristic parameters of the kiln head burner 91 are set as follows:
primary air volume: about 0.05 to 0.08Nm3/kg.cl；
The air volume proportion of the cooling air, the axial flow air and the rotational flow air is as follows: 1:2: 1;
cooling wind speed: 50-100 m/s;
axial flow wind speed: 150-200 m/s;
rotating wind speed: 100 to 150 m/s.
The invention also provides a cement firing method based on pure oxygen combustion, as shown in fig. 4, the firing method comprises the following steps:
firstly, carrying out heat exchange on oxygen produced by a pure oxygen preparation device 1 and high-temperature waste heat produced by a cooler 8 through a heat exchanger 2 to generate high-temperature pure oxygen;
specifically, the pure oxygen preparation device 1 produces the oxygen-containing gas by adopting a low-temperature air separation or pressure swing adsorption mode, wherein the oxygen content in the oxygen-containing gas is more than 95%, and then the produced oxygen and the high-temperature waste heat generated by the cooler 8 are subjected to heat exchange, so that the high-temperature pure oxygen is generated, and the subsequent combustion is facilitated. Exemplarily, the high-temperature waste heat is high-temperature air discharged after the clinker is cooled in the front two chambers of the cooler 8, the temperature of the high-temperature waste heat is 950-1000 ℃, and the air volume is 0.6-0.7 Nm3Cl is about 1/3 of the total cooling air volume of the cooler 8.
Dividing the generated high-temperature pure oxygen into three paths, and respectively conveying the three paths of high-temperature pure oxygen to a decomposing furnace 10 filled with raw materials, a rotary kiln 9 and a kiln head burner 91 for combustion; wherein, the pure oxygen enters the combustor as primary air and does not participate in the coal powder transportation.
Illustratively, the total oxygen air volume generated by the pure oxygen preparation equipment 1 is 0.2-0.25 Nm3Cl, wherein the temperature of the high-temperature pure oxygen after heat exchange can reach 760-800 ℃; the oxygen after heat exchange is divided into three paths to enter a burning system, one path replaces secondary air, and directly enters the rotary kiln 9 through the kiln door cover 92, so that fuel burning in the rotary kiln 9 is met. One path of the air replaces tertiary air to enter the decomposing furnace 10, and combustion supporting is provided for combustion in the decomposing furnace 10. And a path to the kiln head burner 91 as primary air to provide momentum for the rotary kiln 9 to form sufficient flame.
Thirdly, treating the flue gas generated by combustion through a tail gas treatment device 13, and treating the flue gas through CO2Capture device 15 captures CO in flue gas2；
Specifically, the flue gas after combustion in the rotary kiln 9 enters the decomposing furnace 10, and the flue gas in the rotary kiln 9 and CO generated by the decomposing furnace 102After being converged, the mixture enters a kiln tail preheater 11 system pair and enters a decomposing furnace 1Preheating the raw material of 0; finally discharging the flue gas of the firing system in CO2After the collection system 15 is subjected to dust removal, desulfurization, denitration and other processes, CO is formed2The high-purity flue gas with the concentration of more than 80 percent can be directly subjected to adsorption rectification to obtain CO with higher purity (more than 99 percent)2Gas, high purity (over 99%) CO2The gas can be provided for other industrial fields.
And step four, introducing the clinker generated by combustion into the cooling machine 8 for cooling, and performing high-temperature waste heat recovery through the waste heat recovery device 6.
Specifically, clinker is generated in the rotary kiln 9, the clinker enters the cooler 8 from the rotary kiln 9, high-temperature waste heat is generated after cooling, a pipeline of the output high-temperature waste heat is connected with a pure oxygen output pipeline generated by the pure oxygen preparation device 1, heat exchange between the high-temperature waste heat and the generated pure oxygen is realized, the generated pure oxygen is heated, and high-temperature pure oxygen is formed, so that the combustion efficiency is improved; in order to realize the recovery of the waste heat of the cooler 8 and the reasonable utilization of resources, the hot air pipe 4 of the cooler and the waste air pipe 5 of the cooler are connected with the waste heat recovery device 6, and the high-temperature waste heat generated by the cooler 8 is recovered. The pure oxygen is indirectly heated and then directly enters a cement firing system to be used as combustion-supporting gas; the cooling air of the cooler 8 is provided by the blower 7, the oxygen-containing air of the rotary kiln 9 is provided by the pure oxygen preparation device 1, the air utilization of the pure oxygen and the air utilization of the pure oxygen are separated and do not interfere with each other, and the arrangement of the blanking necking 93 can ensure that clinker in the rotary kiln 9 can enter the cooler 8, but hot air in the cooler 8 cannot enter the rotary kiln 9.
The pure oxygen tertiary air entering the decomposing furnace 10 is divided into three but not limited to three, and sequentially enters the bottom of the decomposing furnace 10 to provide combustion-supporting gas, so that the combustion speed of the pulverized coal is controlled, and local high temperature is avoided. Air volume control valves are respectively arranged on three air pipelines (for example, control valves are respectively arranged at the inner part of the tertiary air pipe 12, the joint of the oxygen conveying pipe 3 and the kiln head burner 91, the joint of the oxygen conveying pipe 3 and the decomposing furnace 10 and the joint of the oxygen conveying pipe 3 and the rotary kiln 9), so as to control the air volume of the oxygen introduced into the decomposing furnace 10, the rotary kiln 9 and the kiln head burner 91, and further enhance the control on the air volume entering the decomposing furnace 10, the rotary kiln 9 and the kiln head burner 91. At the bottom of the decomposing furnace 10, two inverted cone structures are arranged, and because the initial smoke volume entering the decomposing furnace is smaller, the material directly falls into the rotary kiln 9, the airflow speed in the decomposing furnace 10 is controlled in a reasonable range through the inverted cone structures, and the material is guaranteed to move upwards along with the airflow.
Due to CO in the decomposing furnace 102High concentration, increasing CaCO in raw material3The decomposition temperature of the decomposing furnace 10 is required to reach the decomposition temperature of more than 950 ℃, so that the casting material in the decomposing furnace 10 is required to adopt a high-temperature refractory material with the temperature resistance of more than 1500 ℃, and the thickness of the refractory material is increased to 200mm so as to reduce the crusting in the decomposing furnace 10.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (9)
1. A cement burning system based on pure oxygen combustion is characterized by comprising a cement burning system,
a pure oxygen preparation device for producing high concentration oxygen;
the oxygen conveying pipe is connected with the pure oxygen preparation device;
the rotary kiln is connected with the oxygen conveying pipe, and the oxygen conveying pipe is used for conveying high-temperature pure oxygen into the rotary kiln; the end part of the rotary kiln is connected with a kiln head burner, the kiln head burner is connected with the oxygen conveying pipe, and the oxygen conveying pipe is used for conveying high-temperature pure oxygen into the kiln head burner;
the tertiary air pipe is communicated with the oxygen conveying pipe;
the decomposing furnace is connected with the tertiary air pipe, and the tertiary air pipe is used for conveying high-temperature pure oxygen into the decomposing furnace to supply fuel for combustion; the decomposing furnace is also connected with the rotary kiln, and the rotary kiln is used for calcining the hot raw meal discharged from the decomposing furnace;
the kiln tail preheater is connected with the decomposing furnace and is used for preheating raw materials;
the high-temperature fan is connected with the kiln tail preheater through a pipeline and used for carrying out traction conveying on flue gas generated after combustion;
the tail gas treatment device is connected with the high-temperature fan and is used for carrying out dust removal, desulfurization and denitration treatment on the conveyed flue gas;
CO2a capture device, the CO2The capture equipment is connected with the tail gas treatment device, and the CO is2The trapping device is used for carrying out CO treatment on the treated flue gas2Trapping;
the cooler is connected with the rotary kiln and is used for cooling clinker output by the rotary kiln;
a blower provided at a side of the cooler, the blower for providing sufficient cooling wind into the cooler;
one end of the cooler hot air pipe is connected with the cooler, and the cooler hot air pipe is used for conveying hot air generated by the front half section of the cooler;
one end of the cooler exhaust pipe is connected with the cooler, and the cooler exhaust pipe is used for conveying hot air generated by the rear half section of the cooler; the cooler hot air pipe and the cooler residual air pipe are arranged at the top of the cooler;
the waste heat recovery device is connected with the tail ends of the hot air pipe of the cooler and the waste air pipe of the cooler and is used for recovering waste heat of the conveyed hot air;
the heat exchanger is connected with the oxygen conveying pipe and the hot air pipe of the cooling machine and used for carrying out heat exchange on pure oxygen and high-temperature waste heat air and preheating the pure oxygen into the high-temperature pure oxygen.
2. The pure oxygen combustion-based cement burning system according to claim 1, wherein said pure oxygen producing means produces a high concentration oxygen-containing gas by means of low temperature air separation or pressure swing adsorption, wherein the oxygen content in said oxygen-containing gas is 95% or more.
3. The pure oxygen combustion based cement firing system as claimed in claim 1 or 2, wherein the kiln tail preheater comprises a multi-stage arrangement of cyclones having a number of stages comprising four stages, five stages or six stages.
4. The pure oxygen combustion-based cement burning system according to claim 1 or 2, wherein the rotary kiln is connected with the cooling machine through a feed throat, and the feed throat is funnel-shaped.
5. The pure oxygen combustion-based cement burning system according to claim 1 or 2, wherein the temperature of air in the hot air pipe of the cooling machine is 950 to 1000 ℃, and the air volume is 0.6 to 0.7Nm3Cl; the air volume of the high-temperature pure oxygen is 0.2-0.25 Nm3Cl, and the temperature is 760-800 ℃ after heat exchange with hot air is completed.
6. The pure oxygen combustion-based cement burning system as claimed in claim 1 or 2, wherein air volume control valves are installed at the connection of the oxygen delivery pipe and the tertiary air pipe, the connection of the oxygen delivery pipe and the kiln head burner, and the connection of the oxygen delivery pipe and the rotary kiln.
7. The pure oxygen combustion-based cement burning system according to claim 1 or 2, wherein the casting material in the decomposing furnace is a high temperature refractory material resistant to 1500 ℃.
8. A cement burning method based on pure oxygen combustion is characterized by comprising the following steps,
carrying out heat exchange on oxygen produced by the pure oxygen preparation device and high-temperature waste heat produced by a cooling machine through a heat exchanger to generate high-temperature pure oxygen;
dividing the generated high-temperature pure oxygen into three paths, and respectively conveying the three paths of high-temperature pure oxygen to a decomposing furnace filled with raw materials, a rotary kiln and a kiln head combustor for combustion;
treating the flue gas generated by combustion by a tail gas treatment device and passing through CO2Trapping equipment for trapping CO in flue gas2；
And (3) introducing the clinker calcined in the rotary kiln into the cooling machine for cooling, and recovering waste heat through a waste heat recovery device.
9. The method for cement calcination based on pure oxygen combustion as claimed in claim 8, wherein the flue gas generated by combustion is treated by a tail gas treatment device and passed through CO2Trapping equipment for trapping CO in flue gas2Comprises the steps of (a) preparing a mixture of a plurality of raw materials,
after the tail gas is treated by the processes of dust removal, desulfurization and denitration, the CO with the concentration of more than 80 percent is obtained2A gas;
the obtained CO is2After the gas is treated by an adsorption and rectification mode, CO with the purity of more than 99 percent is obtained2A gas.
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