CN109631593B - Rotary lime kiln preheater with efficient flue gas desulfurization - Google Patents
Rotary lime kiln preheater with efficient flue gas desulfurization Download PDFInfo
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- CN109631593B CN109631593B CN201910109617.XA CN201910109617A CN109631593B CN 109631593 B CN109631593 B CN 109631593B CN 201910109617 A CN201910109617 A CN 201910109617A CN 109631593 B CN109631593 B CN 109631593B
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- flue gas
- sulfur
- desulfurization
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- lime kiln
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Classifications
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
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- 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
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
The invention relates to a rotary lime kiln preheater with high-efficiency flue gas desulfurization, which comprises a preheater main body, a top stock bin, a blanking pipe, a smoke exhaust pipe, a push rod device, a blanking chute and a sulfur-fixing agent auxiliary agent conveying pipeline, wherein a nozzle is arranged at the lower end of the sulfur-fixing agent auxiliary agent conveying pipeline and is positioned above the blanking chute. According to the invention, through the arrangement of the sulfur-fixing agent auxiliary agent conveying pipeline, sulfur-fixing agent auxiliary agent powder can be conveyed to the nozzle above the blanking chute in the preheater main body through the sulfur-fixing agent auxiliary agent conveying pipeline under the action of high-speed air flow, and is sprayed out through the nozzle to be mixed with high-temperature flue gas flow from the rotary lime kiln, so that the microstructure of the sulfur-fixing agent is improved, the pyrolysis of desulfurization products is delayed, and the decomposition temperature of the desulfurization products is increased.
Description
Technical field:
the invention relates to a lime kiln flue gas desulfurization device, in particular to a rotary lime kiln preheater with efficient flue gas desulfurization.
The background technology is as follows:
at present, the flue gas desulfurization technology mainly comprises a dry method, a semi-dry method and a wet method, and the technical schemes generally adopt a calcium-based desulfurizing agent. Calcium-based desulfurizing agent and SO in flue gas 2 Generation of CaSO 3 Further oxidation to CaSO at high temperature 4 . Thereby making SO 2 The gas is removed from the flue gas and is fixed in the desulfurizing agent.
For lime kiln, the input raw material is limestone mainly containing calcium carbonate, the product is lime mainly containing calcium oxide, and both the lime kiln and the lime kiln have the function of absorbing SO 2 Is a common calcium-based desulfurizing agent.
Currently, the mainstream rotary lime kilns are equipped with vertical preheaters to enable recovery of the residual heat of the high-temperature flue gas emitted during the limestone calcination process. Lime stone is firstly stored in a bin at the top of the lime kiln preheater and enters an annular heating space in the middle of the vertical preheater through a blanking pipe. In the annular heating space, lime stone moves from top to bottom, high-temperature flue gas flows from bottom to top, and heat and mass transfer are carried out while the lime stone and the high-temperature flue gas are in countercurrent. In the falling process of lime stone, limestone particles are gradually heated by high-temperature flue gas to be decomposed, the outer surface of the lime stone particles is decomposed into calcium oxide firstly, and when the lime stone particles reach the vicinity of a conical hopper at the bottom of the preheater, the lime stone particles are heated to about 900-1100 ℃, and 30% of the lime stone particles are decomposed approximately; in the rising process of the flue gas, the heat of the high-temperature flue gas is transferred to lime stone, the temperature of the flue gas gradually decreases in the rising process, and when the flue gas reaches the vicinity of a smoke exhaust pipe at the upper part of the preheater, the temperature of the flue gas is reduced to about 260-300 ℃. Lime stones falling near the conical hopper at the bottom of the preheater are pushed into a discharging chute by a push rod device and enter a rotary kiln for calcination.
During the preheating and descending process of the limestone, the materials collide with each other on the outer surface, and the calcium oxide layer generated on the outermost layer of the materials is crushed into calcium oxide powder. Meanwhile, when the lime stone is calcined in the rotary kiln, the lime stone continuously rolls and rubs against the kiln wall, and a calcium oxide layer generated on the outer side of the lime stone can fall off and break due to collision and friction with the kiln wall to generate a large amount of calcium oxide powder with tiny particle size. Under the impact of high-speed flue gas, calcium oxide powder is dispersed in the flue gas and moves along with the flow of the flue gas, and part of the calcium oxide powder enters a sintered product; part of the dust enters the smoke exhaust pipe and is trapped by dust removing equipment.
Although a great amount of lime is arranged in the lime kiln, and a great amount of calcium oxide powder with small particle size is distributed in the flue gas, the Ca/S ratio in the kiln can be far satisfied with the ratio required by desulfurization, but the desulfurization rate is still lower, and SO in the flue gas is still lower 2 The flue gas desulfurization device is high, cannot meet the requirement of environmental protection, and needs to be additionally provided with additional flue gas desulfurization equipment.
Furthermore, calcium oxide and SO 2 The reaction for producing calcium sulfite is a reversible reaction, and the higher the temperature is, the higher the reaction rate is, but when the temperature is higher than a certain temperature, the decomposition rate of calcium sulfite is higher than the production rate. At high temperature in the presence of O 2 When present, the calcium sulfite produced will be rapidly oxidized to calcium sulfate, which has high temperature stability.
In summary, the low desulfurization rate of calcium oxide is caused by the following factors:
1) Related to the microstructure of calcium oxide: after lime stone reaction is carried out for a period of time, the surface pores of the calcium oxide particles are blocked quickly, thereby preventing SO 2 Diffusion into the inside of the catalyst to reduce the sulfur fixation rate;
2) Calcium oxide and SO 2 Is a gas-solid reaction, and the activity of calcium oxide is reduced along with the progress of the reaction;
3) The sulfur fixation reaction is a reversible process, and the temperature has an important influence on the reaction process. The temperature is low, the reaction speed is low, and the reaction is carried out towards the direction of generating a sulfur fixation product; the temperature is too high, the reaction rate is high, but the decomposition of sulfur-fixing products can occur, and the reaction is towards SO precipitation 2 In particular at temperatures above 1200 ℃ with substantial amounts of SO 2 And (3) precipitation.
The invention comprises the following steps:
in order to overcome the problems, the invention aims at improving the thermal characteristics of the rotary lime kiln, and aims to provide the rotary lime kiln preheater with high-efficiency flue gas desulfurization.
In order to achieve the aim, the invention provides a rotary lime kiln preheater with high-efficiency flue gas desulfurization, which comprises a preheater main body, a top stock bin, a blanking pipe, a smoke exhaust pipe, a push rod device, a blanking chute and a sulfur-fixing agent auxiliary agent conveying pipeline, wherein a nozzle is arranged at the lower end of the sulfur-fixing agent auxiliary agent conveying pipeline, and the nozzle is positioned above the blanking chute.
According to the invention, through the arrangement of the sulfur-fixing agent auxiliary agent conveying pipeline, sulfur-fixing agent auxiliary agent powder can be conveyed to the nozzle above the blanking chute in the preheater main body through the sulfur-fixing agent auxiliary agent conveying pipeline under the action of high-speed air flow, and is sprayed out through the nozzle to be mixed with high-temperature flue gas flow from the rotary lime kiln, so that the microstructure of the sulfur-fixing agent (namely calcium oxide in the rotary lime kiln) is improved, the pyrolysis of a desulfurization product (namely calcium sulfite) is delayed, and the decomposition temperature of the desulfurization product (namely calcium sulfite) is increased.
Further, a sulfur-fixing agent-assisting agent transporting pipe is arranged at the center of the preheater main body.
Through the arrangement, the sulfur fixing agent auxiliary agent and the high-temperature flue gas flow can be uniformly mixed.
Further, the above-mentioned preheater main body includes inner and outer plates that together enclose an annular heating space including a low temperature section, a desulfurization section and a high temperature section, the desulfurization section being arranged so that the cross section becomes larger from top to bottom and then smaller to increase the residence time of the material in the desulfurization section.
Through the arrangement of the structure, the residence time of the materials in the temperature range of 800-900 ℃ in the preheater can be increased.
Still further, the desulfurization section inner plate has a first inclined portion provided so that a horizontal inclination angle thereof is smaller than a stacking angle of the material, and a second inclined portion provided so that a horizontal inclination angle thereof is larger than a friction angle between the material and the inner plate.
By the arrangement of the first and second inclined portions, the movement of the stone can be unaffected and the entire annular heating space can be filled.
Still further, the inner panel is further provided with a vertical portion between the first inclined portion and the second inclined portion.
Still further, the temperature of the desulfurization section is set to 800-900 ℃.
Still further, the rotary lime kiln preheater with high-efficiency flue gas desulfurization further comprises a flue gas rotational flow diversion water spraying device, and the flue gas rotational flow diversion water spraying device is arranged at the inlet end of the smoke exhaust pipe.
A smoke rotational flow diversion water spraying device is additionally arranged at the inlet end of the smoke exhaust pipe, calcium oxide is activated again, the reaction speed of a low-temperature area in the main body of the preheater is increased, and the sulfur fixation rate is improved;
still further, above-mentioned flue gas whirl water conservancy diversion water jet equipment includes solid fixed ring, lower fixed plate, installs on the solid roof down and towards the inside nozzle of flue gas whirl water conservancy diversion water jet equipment, the water pipe of being connected with the nozzle, is fixed in a plurality of guide plates between solid fixed ring and the lower fixed plate, and a plurality of guide plates are around the inside imaginary circle tangential distribution of flue gas whirl water conservancy diversion water jet equipment.
Through the arrangement of the structure, the flowing direction of the flue gas entering the smoke exhaust pipe can be changed by means of arrangement of the guide plates, so that the direction of the flue gas flowing into the smoke exhaust pipe is changed from the axial direction of the smoke exhaust pipe to the tangential direction of the smoke exhaust pipe, the contact time of calcium oxide and the flue gas can be increased 1), and the heat and mass transfer of water drops and the flue gas can be accelerated 2).
Still further, the plurality of baffles are uniformly distributed along a tangential direction of the inner imaginary circle.
Further, the radius of the inner imaginary circle is half of the radius of the smoke exhaust pipe.
This arrangement enables the flue gas to form a strong swirling flow in the flue gas swirling flow water jet device.
These and other aspects of the invention will be apparent from and elucidated with reference to the embodiments described hereinafter.
Description of the drawings:
the structure of the invention, as well as further objects and advantages thereof, will be better understood by reference to the following description taken in conjunction with the accompanying drawings in which like reference numerals identify like elements:
FIG. 1 is a schematic view of the internal structure of a rotary lime kiln preheater with efficient flue gas desulfurization in accordance with an embodiment of the present invention;
FIG. 2 is a schematic view of the annular heating space of the rotary lime kiln preheater with efficient flue gas desulfurization of FIG. 1, which clearly shows the structure of the annular heating space in which the cross section of the desulfurization section is enlarged from top to bottom and then reduced;
FIG. 3 is a flow-directing water jet apparatus for swirling flue gas from the rotary lime kiln preheater shown in FIG. 1 with efficient flue gas desulfurization.
The specific embodiment is as follows:
specific embodiments of the present invention will be described below with reference to the accompanying drawings.
As shown in fig. 1, the rotary lime kiln preheater with efficient flue gas desulfurization according to an embodiment of the present invention comprises a top bin 1, a preheater main body 2, a blanking pipe 3, a smoke exhaust pipe 4, a push rod device 5, a blanking chute 6, and a sulfur-fixing agent auxiliary agent conveying pipeline 7, wherein a nozzle 70 is arranged at the lower end of the sulfur-fixing agent auxiliary agent conveying pipeline 7, and the nozzle 70 is positioned above the blanking chute 6. Preferably, the sulfur-fixing agent-auxiliary feed duct 7 is arranged in the central position of the preheater main body 2.
As shown in fig. 1, and referring to fig. 2 and 3, the preheater body 2 includes an inner plate 21 and an outer plate 22 that together enclose an annular heating space 20. The annular heating space 20 includes a low temperature section, a desulfurization section, and a high temperature section, the desulfurization section being configured to be enlarged and then reduced in cross section from top to bottom (see fig. 2) to increase the residence time of the material within the desulfurization section. In the desulfurization section (temperature 800 to 900 ℃), the inner plate 21 has a first inclined portion 210, a vertical portion 211, and a second inclined portion 212, the first inclined portion 210 is disposed so that the horizontal inclination angle α thereof is smaller than the stacking angle of the material, and the second inclined portion 212 is disposed so that the horizontal inclination angle β thereof is larger than the friction angle between the material and the inner plate, as shown in fig. 3.
As shown in fig. 1 and referring to fig. 3, in the present embodiment, the rotary lime kiln preheater further includes a flue gas cyclone diversion water spray device 8, and the flue gas cyclone diversion water spray device 8 is installed at the inlet end of the smoke exhaust pipe 4. As shown in fig. 3, the flue gas swirling flow guiding water spraying device 8 comprises an upper fixing ring 81, a lower fixing plate 83, a nozzle 85 arranged on the lower fixing top plate 83 and facing the inside of the flue gas swirling flow guiding water spraying device 8, a water pipe 87 connected with the nozzle 85, and a plurality of guide plates 82 fixed between the upper fixing ring 81 and the lower fixing plate 83. The plurality of baffles 82 are distributed tangentially uniformly about an inner imaginary circle (not shown) of the flue gas swirling flow deflector spray. In the present embodiment, the radius of the inner imaginary circle is half of the radius of the smoke exhaust pipe 4, however, this is just one example, and other values about the "half" may be set, so long as the smoke can form strong swirling flow in the smoke swirling flow guiding water spraying device 8, and too small or too large swirling flow is unfavorable.
In general, in view of the phenomenon of low desulfurization rate of calcium oxide in the prior art, the measures adopted in this embodiment are as follows: 1) The sulfur-fixing agent auxiliary agent is sprayed above the blanking chute 6 through a sulfur-fixing agent auxiliary agent conveying pipeline 7, some sulfur-fixing agent auxiliary agents can improve the microstructure of sulfur-fixing agent (namely calcium oxide), and other sulfur-fixing agent auxiliary agents can delay pyrolysis of desulfurization products (namely calcium sulfite) and improve the decomposition temperature of the desulfurization products; 2) The smoke rotational flow diversion water spraying device 8 is additionally arranged at the inlet end of the smoke exhaust pipe 4 to activate calcium oxide again, so that the reaction speed of the low-temperature section in the annular heating space 20 is increased, and the sulfur fixation rate is improved; 3) The structure of the annular heating space 20 in the preheater body 2 is changed, the volume of the optimum temperature zone is increased, and the residence time of the material in this temperature zone is increased.
Specific operation measures of the steps 1) to 3) are as follows:
1) The ground sulfur-fixing agent auxiliary agent powder is conveyed to a nozzle 70 above the blanking chute 6 of the high-temperature section of the annular heating space 20 through a sulfur-fixing agent auxiliary agent conveying pipeline 7 under the action of high-speed air flow, and the air flow carrying the sulfur-fixing agent auxiliary agent powder is uniformly mixed with the high-temperature flue gas flow from the rotary kiln.
The auxiliary agent for improving the microstructure of the sulfur-fixing agent generally comprises an alkali metal compound and an organic solution, and the addition of the auxiliary agent can improve the micropore diameter, pore internal structure, pore specific surface area, pore distribution and the like of the sulfur-fixing agent, thereby improving the activity of the sulfur-fixing agent and further improving the sulfur-fixing rate. Wherein the alkali metal compound auxiliary agent mainly comprises Na 2 CO 3 、NaCl、KCl。Na 2 CO 3 The addition of (2) can promote CaO lattice rearrangement, improve the distribution of pores and the size of pores, and inhibit the pyrolysis of sulfur-fixing products. The presence of NaCl and KCl increases the efficiency of CaO in the sulfur fixation process because a thin layer of NaCl/CaO is formed during the reaction, and KCl/CaO is low in eutectic layer, and the migration and diffusion capacity of sodium and potassium ions are increased, so that the lattice structure of CaO is changed, and the CaO property is improved.
Sulfur-fixing agent additives are added to the sulfur-fixing agent to form a catalyst having a high temperatureThermally stable sulfur-containing minerals or forming low temperature eutectic encapsulation and preventing CaSO 4 A decomposed additive. The sulfur-fixing agent auxiliary agents mainly comprise:
the addition of the iron and silicon components can generate a Ca-Fe-Si-O system to form a heat-resistant silicate stable phase, and the calcium sulfate is covered or wrapped by the high-melting silicate, so that the re-decomposition of the calcium sulfate is effectively prevented, and the desulfurization rate at high temperature can be obviously improved;
Fe 2 O 3 the reaction rate of calcium oxide and sulfur dioxide is accelerated, and calcium sulfite is easy to oxidize into calcium sulfate at high temperature;
Al 2 O 3 can also inhibit pyrolysis of sulfur-fixing product, and can form product with high thermal stabilityAnd the product can cover or encapsulate Ca S O 4 The surface of the crystal inhibits the decomposition of the crystal, and effectively improves the sulfur fixation effect;
MgO plays a role in promoting the sulfur fixation reaction of CaO and can catalyze the lime sulfur fixation reaction;
therefore, the main component of the sulfur-fixing agent auxiliary agent is Al 2 O 3 、SiO 2 、MgO、Fe 2 O 3 A trace amount of an alkali metal compound is used as an auxiliary component.
The sprayed sulfur-fixing agent auxiliary agent is calculated according to the sulfur content in the flue gas and the Ca/S ratio of 2, and the total CaO amount required for absorbing sulfur in the flue gas is calculated reversely, and the auxiliary agent amount is calculated according to the total CaO amount required by 2-6%.
2) The smoke rotational flow diversion water spraying device 8 is additionally arranged at the inlet end of the smoke exhaust pipe 4 in the annular heating space 20 of the rotary lime kiln preheater, which can lead to the following:
the method comprises the steps of activating lime desulfurization reaction, and increasing reaction speed;
the flow direction of flue gas entering in the smoke exhaust pipe 4 is changed: the direction of the flue gas flowing into the smoke exhaust pipe 4 is changed from the axial direction along the smoke exhaust pipe 4 to the tangential direction along the smoke exhaust pipe 4, so that the following benefits are achieved:
a) The speed of the particles in the vertical direction is reduced, and as the particles are influenced by gravity, part of the particles wrapped in the flue gas correspondingly fall into the upper space of the preheater under the action of gravity, so that the contact time of calcium oxide and the flue gas is increased;
b) Under the action of the guide plate 82, the flue gas makes high-speed rotational flow movement in the smoke exhaust pipe 4, the flue gas and water are mixed more uniformly, the heat and mass transfer of water drops and the flue gas are accelerated, the reaction of calcium oxide, water drops and sulfur dioxide in the flue gas is promoted, and the agglomeration of lime powder in the flue gas due to water absorption is avoided to block the smoke exhaust pipe 4;
c) The sprayed water drops are all sucked into the pipeline through the smoke exhaust pipe 4 under the negative pressure of the smoke exhaust pipe 4, so that the influence of the sprayed water drops on the preheating of lime stones is avoided.
3) Changing the structure of the body of the preheater
The optimum temperature range of the sulfur fixation reaction is 800-900 ℃. The temperature exceeds 900 ℃, partial sulfur fixation products can be decomposed, and the total sulfur fixation rate is reduced; the temperature is lower than 800 ℃, the reaction rate is reduced, and the rapid sulfur fixation reaction is not facilitated.
The traditional preheater structure is formed by stretching an annular section surrounded by an inner dodecagon and an outer dodecagon to a certain height, the flue gas flows in a uniform section in the space, the 800-900 ℃ area with the greatest influence on the whole desulfurization reaction only occupies a small part of the whole material layer, the flue gas flow passes through the area at a high speed, the residence time is short, and the desulfurization rate is low.
In order to solve the problem, the invention designs a novel preheater structure, namely: in the area of 800-900 deg.c of lime stone, the main body of the preheater is made of ring structure with constant cross section and with variable cross section, and the horizontal cross section of the area is first enlarged and then reduced and finally returned to original size to raise the residence time of stone in the area of 800-900 deg.c. In the cross-sectional design, firstly, considering the influence of the pile angle of the stone, the horizontal inclination angle α of the first inclined portion 210 should be slightly smaller than the pile angle of the stone; second, in order not to affect the falling of the stone, the horizontal inclination angle β of the second inclination portion 212 should be slightly larger than the friction angle of the stone in consideration of the influence of the friction angle of the stone.
In addition, it should be noted that the height of the material level can be adjusted by increasing the height of the preheater, i.e., increasing the height of the annular heating space 20.
The overall height of the material layer in the annular heating space 20 inside the preheater can be controlled by changing the feeding and discharging amount (for example, by adjusting the movement frequency of the push rod device 5) during the actual production process by increasing the allowance in the height direction of the preheater during the design and manufacturing process of the preheater. Increasing the feeding amount and decreasing the discharging amount will increase the total height of the material layer, resulting in increasing the gap resistance of the material layer, decreasing the flow rate of the flue gas, and further prolonging the residence time of the flue gas in the desulfurization section of the annular heating space 20; conversely, decreasing the feed amount and increasing the discharge amount will decrease the total height of the material layer, decrease the gap resistance of the material layer, increase the flow rate of the flue gas, and further shorten the residence time of the flue gas in the desulfurization section of the preheater.
The present embodiment has the following advantages:
the smoke rotational flow diversion water spraying device 8 is arranged at the inlet of the smoke exhaust pipe 4, the temperature of the smoke is about 260-300 ℃, water drops can absorb the heat of the smoke to evaporate, and meanwhile, lime powder can not become pasty and agglomerate due to water absorption. Moreover, because the temperature of the flue gas is not high, water drops can stay for enough time to activate desulfurization reaction;
the flue gas cyclone diversion water spraying device 8 changes the mode that the flue gas enters the flue gas exhaust pipe 4 from the original axial entering mode to the tangential entering mode, the mixing of the flue gas, water drops and lime powder is more uniform and strong, the heat and mass transfer resistance of the water drops and the flue gas is smaller, and the flue gas desulfurization effect at low temperature is better;
due to entrainment of the flue gas flow, water drops cannot enter the annular heating space 20 of the preheater, the heat and mass transfer process of limestone in the annular heating space 20 cannot be influenced, and no additional influence is brought to lime production;
because the water spraying area only exists in the flue gas rotational flow diversion water spraying device 8, the water spraying amount can be less, and the influence on the flue gas temperature drop is less;
the inner wall structure of the preheater is changed, so that the residence time of the flue gas and stones in the 800-900 ℃ region, namely the desulfurization section, is more, and the residence time in the optimal desulfurization section is more, thus the overall desulfurization efficiency can be remarkably improved;
the addition of the sulfur-fixing agent auxiliary agent in the high-temperature section of the annular heating space 20 improves the microscopic pore structure of the sulfur-fixing agent, is beneficial to sulfur-fixing reaction, and simultaneously covers the surface of the sulfur-fixing product with substances with high temperature stability, so that the re-decomposition temperature of the sulfur-fixing product is reduced, and the decomposition temperature of the sulfur-fixing product is increased;
the design of the variable cross-section structure of the desulfurization section of the annular heating space 20 of the preheater takes into account the accumulation angle of the stones and the friction angle between the stones and the inner plate, and the stones can better fill the annular heating space 20 of the whole preheater in the falling process;
the design and the manufacture of the preheater take the surplus of the height of the material layer into consideration, and the balance between the feeding and the discharging of the preheater is adjusted according to the requirement during actual production, so that the height of the material layer in the preheater is adjusted.
While the technical content and features of the present invention have been disclosed above, it will be understood that various changes and modifications to the above-described structure, including combinations of technical features individually disclosed or claimed herein, and other combinations of these features as apparent to those skilled in the art may be made under the inventive concept of the present invention. Such variations and/or combinations fall within the technical field to which the invention relates and fall within the scope of the claims of the invention.
Claims (8)
1. The utility model provides a gyration lime kiln pre-heater with high-efficient flue gas desulfurization, its includes pre-heater main part, top feed bin, unloading pipe, exhaust pipe, pusher device, unloading chute, its characterized in that still includes sulfur-fixing agent auxiliary agent pipeline, and this sulfur-fixing agent auxiliary agent pipeline's lower extreme is provided with the nozzle, and this nozzle is located the top of unloading chute, the pre-heater main part includes the inner panel and the planking that enclose into annular heating space jointly, and this annular heating space includes low temperature section, desulfurization section and high temperature section, and this desulfurization section sets up to become bigger earlier than diminishing in order to increase the residence time of material in this desulfurization section from top to bottom, in desulfurization section the inner panel has first tilting portion and second tilting portion, first tilting portion sets up its horizontal tilt angle and is less than the angle of piling up of material, the second tilting portion sets up its horizontal tilt angle and is greater than the material with the friction angle between the inner panel.
2. The rotary lime kiln preheater with efficient flue gas desulfurization of claim 1, wherein the sulfur-fixing agent adjunct delivery conduit is disposed in a central location of the preheater body.
3. The rotary lime kiln preheater with efficient flue gas desulfurization of claim 1, wherein the inner plate is further provided with a vertical portion between the first and second inclined portions.
4. The rotary lime kiln preheater with efficient flue gas desulfurization according to claim 1, wherein the temperature of the desulfurization section is set at 800-900 ℃.
5. The rotary lime kiln preheater with efficient flue gas desulfurization according to any of claims 1 to 4, further comprising a flue gas swirling flow diversion water spray device mounted at the inlet end of the flue gas fume tube.
6. The rotary lime kiln preheater with efficient flue gas desulfurization as recited in claim 5, wherein said flue gas swirling flow diversion water spray device comprises an upper fixed ring, a lower fixed plate, a nozzle mounted on the lower fixed top plate and directed toward the interior of said flue gas swirling flow diversion water spray device, a water pipe connected to the nozzle, a plurality of deflectors fixed between the upper fixed ring and the lower fixed plate, the plurality of deflectors being tangentially distributed around an interior imaginary circle of said flue gas swirling flow diversion water spray device.
7. The rotary lime kiln preheater with efficient flue gas desulfurization of claim 6, wherein said plurality of baffles are tangentially uniformly distributed along said inner imaginary circle.
8. The rotary lime kiln preheater with efficient flue gas desulfurization of claim 7, wherein the radius of the inner imaginary circle is half the radius of the flue gas discharge tube.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910109617.XA CN109631593B (en) | 2019-02-11 | 2019-02-11 | Rotary lime kiln preheater with efficient flue gas desulfurization |
| PCT/CN2019/115227 WO2020164259A1 (en) | 2019-02-11 | 2019-11-04 | Rotary lime kiln preheater with efficient flue gas desulfurization |
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| CN109631593B (en) * | 2019-02-11 | 2023-09-26 | 江苏中圣园科技股份有限公司 | Rotary lime kiln preheater with efficient flue gas desulfurization |
| CN116332667A (en) * | 2023-04-06 | 2023-06-27 | 中国科学院过程工程研究所 | Method for preparing porous material and solidifying sulfur from sulfur-containing solid waste |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20040007880A (en) * | 2002-07-11 | 2004-01-28 | 주식회사 포스코 | Rotary kiln having controlling system for hot gas in kiln |
| CN104651564A (en) * | 2015-02-13 | 2015-05-27 | 唐竹胜 | Method for reducing and separating granular iron rapidly at low temperature |
| CN104876456A (en) * | 2015-05-16 | 2015-09-02 | 江苏中圣园科技股份有限公司 | Rotary kiln lime roasting process |
| CN107174927A (en) * | 2017-07-13 | 2017-09-19 | 北京建筑材料科学研究总院有限公司 | The method of denitration and system of a kind of cement rotary kiln |
| CN209512528U (en) * | 2019-02-11 | 2019-10-18 | 江苏中圣园科技股份有限公司 | Revolution limekiln preheater with high-efficiency flue gas desulfurization |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3759116B2 (en) * | 2003-03-28 | 2006-03-22 | 株式会社プランテック | Vertical waste incinerator for waste incineration and control method thereof |
| CN102974207B (en) * | 2012-11-07 | 2015-02-18 | 环境保护部华南环境科学研究所 | Method and apparatus for cement rotary kiln flue gas denitration and desulfurization |
| CN103896501B (en) * | 2013-12-30 | 2016-03-16 | 辽宁劲达华杰工程技术有限公司 | A kind of lime production line kiln tail ventilation system and kiln tail ventilation technics |
| CN104792154B (en) * | 2015-04-03 | 2017-01-25 | 石家庄新华能源环保科技股份有限公司 | Dividing wall type rotary kiln device |
| CN205760546U (en) * | 2016-05-12 | 2016-12-07 | 南京凯盛国际工程有限公司 | Cement kiln desulphurization system |
| CN206138996U (en) * | 2016-09-19 | 2017-05-03 | 中材国际环境工程（北京）有限公司 | Novel cement kiln semi -dry desulfurization system |
| CN107754591A (en) * | 2017-11-20 | 2018-03-06 | 上海三融环保工程有限公司 | A kind of high-efficient atomizing desulfurizer and method |
| CN107930376A (en) * | 2017-11-27 | 2018-04-20 | 浙江工业大学 | The cement kiln desulfurizer and technique of a kind of dry-and-wet combined |
| CN108686494A (en) * | 2018-06-21 | 2018-10-23 | 北京中丹科技有限公司 | With the calcium oxide in kiln exit gas to the method and its system of kiln exit gas desulfurization |
| CN109631593B (en) * | 2019-02-11 | 2023-09-26 | 江苏中圣园科技股份有限公司 | Rotary lime kiln preheater with efficient flue gas desulfurization |
-
2019
- 2019-02-11 CN CN201910109617.XA patent/CN109631593B/en active Active
- 2019-11-04 WO PCT/CN2019/115227 patent/WO2020164259A1/en active Application Filing
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20040007880A (en) * | 2002-07-11 | 2004-01-28 | 주식회사 포스코 | Rotary kiln having controlling system for hot gas in kiln |
| CN104651564A (en) * | 2015-02-13 | 2015-05-27 | 唐竹胜 | Method for reducing and separating granular iron rapidly at low temperature |
| CN104876456A (en) * | 2015-05-16 | 2015-09-02 | 江苏中圣园科技股份有限公司 | Rotary kiln lime roasting process |
| CN107174927A (en) * | 2017-07-13 | 2017-09-19 | 北京建筑材料科学研究总院有限公司 | The method of denitration and system of a kind of cement rotary kiln |
| CN209512528U (en) * | 2019-02-11 | 2019-10-18 | 江苏中圣园科技股份有限公司 | Revolution limekiln preheater with high-efficiency flue gas desulfurization |
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| CN109631593A (en) | 2019-04-16 |
| WO2020164259A1 (en) | 2020-08-20 |
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