CN210752074U - Calcium circulation dry desulphurization system for cement clinker production line - Google Patents
Calcium circulation dry desulphurization system for cement clinker production line Download PDFInfo
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- CN210752074U CN210752074U CN201920856111.0U CN201920856111U CN210752074U CN 210752074 U CN210752074 U CN 210752074U CN 201920856111 U CN201920856111 U CN 201920856111U CN 210752074 U CN210752074 U CN 210752074U
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Abstract
The utility model discloses a cement clinker production line calcium circulation dry desulphurization system, which belongs to the technical field of flue gas desulphurization, and comprises a decomposition unit for decomposing raw materials into active hot raw materials, wherein the decomposition unit comprises a multi-stage kiln tail preheater and a decomposition furnace; the desulfurizer preparation unit and the desulfurizer conveying unit are also included; the desulfurizer preparation unit comprises a cooling unit connected with a discharge port of the decomposition unit and a digestion unit connected with a discharge port of the cooling unit; the digestion sheetThe discharge port of the unit is connected with a desulfurizer conveying unit, and the desulfurizer conveying unit is connected with a kiln tail preheater. The system adopts hot raw materials self-made by a cement kiln, and active raw materials after cooling and digestion are fed into a kiln tail preheater as a desulfurizing agent, and the desulfurizing agent reacts with kiln tail flue gas to remove SO in the flue gas2Thereby reducing SO in the tail flue gas of the kiln2Content, realizes self-sufficiency of desulfurizer and solves the problem of flue gas SO2The discharge problem and the cost of the purchased desulfurizer are saved.
Description
Technical Field
The utility model relates to a flue gas desulfurization technical field especially relates to a cement clinker production line calcium circulation dry process desulfurization system.
Background
The cement raw materials mainly comprise calcium raw materials, silicon-aluminum raw materials, iron raw materials and the like, wherein the calcium raw materials are mainly used and generally account for about 80 percent. In the production process of cement clinker, when the raw material contains more low-valence sulfur such as organic sulfur or sulfide, the low-valence sulfur is released to generate SO by high-temperature oxidation in the preheater2Gas, resulting in SO in the flue gas2The concentration exceeds the standard, and the environmental-friendly emission index can be reached only by carrying out desulfurization treatment.
The existing cement kiln flue gas desulfurization methods mainly comprise dry desulfurization, wet desulfurization and the like, and the desulfurizing agent is mainly purchased from the outside. The dry desulfurization system is simple, the running power consumption is low, the adopted desulfurizer is calcium hydroxide or sodium bicarbonate and the like, the desulfurizer is fed to the positions of an air pipe and the like of a kiln tail preheater, the desulfurizer reacts with sulfur dioxide in flue gas to carry out desulfurization, but the desulfurization efficiency is often lower, and the dry desulfurization system is not suitable for a cement production line with high sulfur dioxide background concentration.
The cement kiln flue gas can also adopt a wet desulphurization process, wherein the most common wet desulphurization method is a lime/gypsum method, namely limestone is adopted as a desulfurizer, the limestone is mixed with water to prepare slurry, the slurry is sprayed into a desulphurization tower, and the lime slurry absorbs sulfur dioxide in the flue gas to react to generate gypsum. Wet desulfurization has the problems of white smoke, gypsum rain, chimney corrosion and the like, and has large water consumption, the wastewater needs to be treated, and the whole treatment cost is higher.
Compared with wet desulphurization, the semi-dry flue gas desulphurization technology has the advantages of clean smoke, no white smoke, no gypsum rain, low water consumption, no wastewater treatment, small corrosion to a chimney and the like, but the power consumption of the operation of a desulphurization system is relatively high. The existing semi-dry desulfurization technology needs an external desulfurizer (quicklime or hydrated lime), the cost of the desulfurizer is high, the desulfurized slag is difficult to dispose, and the technology has no engineering application in the cement industry. The technical principle of the semi-dry desulfurization method is as follows: SO in flue gas2And the desulfurizing agent and water in the circulating fluidized bed desulfurizing tower are subjected to ionic chemical reaction to generate desulfurization products such as calcium sulfite and the like. The desulfurizer is highly enriched under the external circulation system of the dust collector to realize SO in the flue gas2The removal is efficient.
In summary, when the background concentration of sulfur dioxide in the cement production line is low, dry desulfurization can be adopted, but a desulfurizing agent needs to be purchased externally, carbonization easily occurs in the transportation and storage processes, lime is converted into calcium carbonate, and the activity of the desulfurizing agent is reduced. Therefore, the calcium circulation dry desulphurization system for the cement clinker production line provides the desulfurizer prepared by the production line for the dry desulphurization system, and has important significance for popularization and application of the cement kiln flue gas desulphurization technology with high efficiency, low cost and no waste residue.
Disclosure of Invention
An object of the utility model is to provide a cement clinker production line calcium cycle dry desulfurization system, this dry desulfurization system will be through the thermal raw material of dore furnace decomposition, through corresponding cooling, digestion after in desulfurizer conveying unit feeding kiln tail pre-heater, absorb the sulfur dioxide that produces in the cement kiln clinker production process, save the cost of purchasing the desulfurizer outward, the system operation power consumption is low, reduces lime ore resource consumption.
The utility model is realized in such a way, a cement clinker production line calcium circulation dry desulphurization system comprises a decomposition unit for decomposing raw materials into active hot raw materials, wherein the decomposition unit comprises a multi-stage kiln tail preheater and a decomposition furnace; the desulfurizer preparation unit and the desulfurizer conveying unit are also included; the desulfurizer preparation unit comprises a cooling unit connected with a discharge port of the decomposition unit and a digestion unit connected with a discharge port of the cooling unit; and a discharge port of the digestion unit is connected with a desulfurizer conveying unit, and the desulfurizer conveying unit is connected with a kiln tail preheater.
Preferably, the cooling unit is connected with a cyclone discharge pipe of the last-stage kiln tail preheater through a material taking unit; the material taking unit comprises a material distributing pipe, a high-temperature gate valve I and a high-temperature rotary discharger, wherein the high-temperature gate valve I and the high-temperature rotary discharger are arranged on the material distributing pipe, one end of the material distributing pipe is connected with a cyclone discharging pipe of the last-stage kiln tail preheater, and the other end of the material distributing pipe is connected with the cooling unit.
Preferably, the cooling unit is connected with an outlet air pipe of the decomposing furnace through a material taking unit; the material taking unit comprises a material taking cyclone, a high-temperature gate valve II is arranged on an inlet pipeline of the material taking cyclone, and a high-temperature gate valve III is arranged on an outlet air pipe of the material taking cyclone; the inlet pipeline of the material taking cyclone is connected with an outlet air pipe of the decomposing furnace, the outlet air pipe of the material taking cyclone is connected with an outlet air pipe of a last-stage or penultimate-stage kiln tail preheater, and the discharging pipe of the material taking cyclone is connected with the cooling unit.
Preferably, the cooling unit is a two-stage suspension cooling.
Preferably, the cooling unit comprises a first-stage cyclone and a second-stage cyclone, the other end of the material separating pipe of the material taking unit is connected with an outlet air pipe of the first-stage cyclone, the outlet air pipe of the first-stage cyclone is connected with an inlet of the second-stage cyclone, a discharging pipe of the second-stage cyclone is connected with the inlet of the first-stage cyclone, cooling air is introduced into the inlet of the first-stage cyclone, and the outlet air pipe of the second-stage cyclone is connected with the waste gas treatment system through a fan.
The second-stage cyclone blanking pipe is also connected with a material distribution pipe positioned at the upper part of the high-temperature gate valve, and a material distribution valve is arranged at the branch of the second-stage cyclone blanking pipe.
Preferably, the cooling unit comprises a first-stage cyclone and a second-stage cyclone, a material-taking cyclone blanking pipe of the material-taking unit is connected with an outlet air pipe of the first-stage cyclone, the outlet air pipe of the first-stage cyclone is connected with an inlet of the second-stage cyclone, the second-stage cyclone blanking pipe is connected with an inlet of the first-stage cyclone, cooling air is introduced into the inlet of the first-stage cyclone, and the outlet air pipe of the second-stage cyclone is connected with the waste gas treatment system through a fan.
Further preferably, the feed opening of the first-stage cyclone is connected with a material collecting bin, a discharge opening of the material collecting bin is provided with a first gate valve and a screw feeder with a meter, and an outlet of the screw feeder with the meter is connected with the digestion unit.
Preferably, the digestion mode of the digestion unit is dry digestion; and an exhaust port of the digestion unit is connected with a cement kiln flue gas and waste gas treatment system through an air pipe of the cooling unit.
Preferably, the digestion unit is also provided with a quicklime feeding port.
Preferably, the desulfurizer conveying unit comprises a Roots blower, a desulfurizer bin, a gate valve II, a rotary feeder, a conveying chute and a lifter which are sequentially connected through a conveying pipeline, a discharge port of the digestion unit is connected with the conveying pipeline between the Roots blower and the desulfurizer bin, and the desulfurizer discharged by the lifter is fed into the kiln tail preheater.
The utility model has the advantages of it is following and beneficial effect:
1. the utility model discloses utilize the cement kiln to have the active characteristics of high desulfurization through the hot raw material of dore decomposition, establish cement clinker production line calcium circulation dry desulfurization system, adopt the cement kiln from heating the raw material, cool off the high temperature material earlier, carry out the digestion increase to the material again, can make the digestibility of calcium oxide in the material reach more than 90%, in order to prepare high activity desulfurizer, realize that the desulfurizer is self-sufficient, thereby partly or whole substitute the outsourcing desulfurizer, solve the flue gas sulfur dioxide emission problem, save the cost of outsourcing desulfurizer, reduce lime ore resource consumption;
2. the utility model discloses a cement clinker production line calcium circulation dry desulfurization system scheme adopts the self-made hot raw meal of cement kiln, and active raw meal after cooling, digestion is as the desulfurizer through desulfurizer conveying element feeding kiln tail in advanceThe heat device, the desulfurizer and the kiln tail flue gas react to remove SO in the flue gas2Thereby reducing SO in the tail flue gas of the kiln2Content (c);
3. the utility model discloses a production of normal production line is not influenced in calcium circulation dry process desulfurization system's operation, and the system is simple, and manufacturing cost and running cost are low, convenient operation.
Drawings
FIG. 1 is a flow chart of a dry desulfurization system according to a first embodiment of the present invention;
FIG. 2 is a flow chart of the cooling and digestion provided by the first embodiment of the present invention by taking the material from the cyclone discharge pipe of the last stage kiln tail preheater;
FIG. 3 is a first flow chart of the cooling and digestion by taking the material from the outlet air duct of the decomposing furnace according to the second embodiment of the present invention;
FIG. 4 is a second flow chart of the cooling and digestion by taking the material from the outlet air duct of the decomposing furnace according to the second embodiment of the present invention;
fig. 5 is a flowchart of a system provided in the third embodiment of the present invention;
fig. 6 is a flowchart of a system according to a fourth embodiment of the present invention.
In the figure: 10-a decomposition unit; 101-a decomposing furnace; 102-cyclone of last stage kiln tail preheater; 103-a cyclone of a penultimate kiln tail preheater; 104-cyclone of last but one stage kiln tail preheater;
20-a cooling unit; 201-first stage cyclone cylinder; 202-second stage cyclone; 203-a fan; 204-an exhaust gas treatment system; 205-a distributing valve; 206-aggregate bin; 207-a gate valve I; 208-a screw feeder with a meter;
30-a digestion unit; 301-quicklime feed inlet;
401-material separating pipe; 402-high temperature gate valve one; 403-high temperature rotary discharger; 404-a take off cyclone; 405-a high-temperature gate valve II; 406-high temperature gate valve three;
50-a rotary kiln;
60-a desulfurizer conveying unit, 601-a Roots blower; 602-desulfurizing agent bin; 603-a transport chute; 604-a hoist; 605-a gate valve II; 606-a rotary feeder; 607-a delivery chute; 608-purchased desulfurizer charging port.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail with reference to the following embodiments and accompanying drawings. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected" and "connected" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1
Referring to fig. 1, an embodiment of the present invention provides a calcium circulation dry desulfurization system for a cement clinker production line, including a decomposition unit 10 for decomposing raw materials into active hot raw materials, where the decomposition unit 10 includes a multi-stage kiln tail preheater and a decomposition furnace 101, the kiln tail preheater selects from three to seven stages of kiln tail preheaters, and a five-stage preheater is preferably adopted in this embodiment; also comprises a desulfurizer preparation unit and a desulfurizer conveying unit 60; the desulfurizer preparation unit utilizes part of the hot raw materials decomposed by the decomposition unit to prepare the desulfurizer through cooling and digestion, and comprises a cooling unit 20 connected with a discharge port of the decomposition unit 10 and a digestion unit 30 connected with a discharge port of the cooling unit 20; the discharge port of the digestion unit 30 is connected with a desulfurizer conveying unit 60, and the desulfurizer conveying unit 60 is connected with a kiln tail preheater. The working principle of the technical scheme is as follows: the raw material is decomposed at high temperature by the decomposition unit 10 to obtain active raw material, the collected active raw material is cooled by the cooling unit 20 to the temperature of within 150 ℃ from 800-950 ℃, and the active raw material is cooledThe active raw material is digested by the digestion unit 30, calcium hydroxide is generated by calcium oxide reaction, the digested active raw material is fed into the kiln tail preheater through the desulfurizer conveying unit 60, and the digested active raw material is used as a desulfurizer to react with kiln tail flue gas to remove SO in the flue gas2Thereby reducing SO in the tail flue gas of the kiln2And (4) content. In general, the desulfurizer is prepared by cooling and digesting the cement kiln self-heating raw materials and absorbing sulfur dioxide generated in the cement kiln clinker production process, so that the purpose of partially or completely replacing the purchased desulfurizer is achieved, the cost of the purchased desulfurizer is saved, the lime ore resource consumption is reduced, and the problem of flue gas sulfur dioxide emission is solved by using the characteristics of a kiln system.
Referring to fig. 2, the cooling unit 20 is connected to a discharge pipe of the cyclone 102 of the final kiln tail preheater through a material taking unit. After the raw meal is calcined in the decomposing furnace 101, calcium carbonate in the raw meal is decomposed at high temperature into calcium oxide, and the high-temperature calcined raw meal is referred to as active raw meal. The active raw materials enter the cyclone 102 of the last-stage kiln tail preheater along with the flue gas, gas-solid separation is carried out through the cyclone 102 of the last-stage kiln tail preheater, most of the active raw materials are collected, and a small part of the active raw materials exit the cyclone 102 of the last-stage kiln tail preheater along with the flue gas and enter the last-stage kiln tail preheater. A portion of the active raw material collected by the cyclone 102 of the final kiln tail preheater enters the cooling unit 20 through the take-off unit for cooling and another portion returns to the rotary kiln 50. Active raw materials subjected to gas-solid separation by the cyclone 102 of the last-stage kiln tail preheater are easier to collect, and the material taking unit is convenient to take materials.
The material taking unit comprises a material distributing pipe 401, a high-temperature gate valve I402 and a high-temperature rotary discharger 403, wherein the high-temperature gate valve I402 is arranged on the material distributing pipe, one end of the material distributing pipe 401 is connected with a material discharging pipe of a cyclone cylinder 102 of the last-stage kiln tail preheater, and the other end of the material distributing pipe 401 is connected with the cooling unit 20. When the material needs to be taken, the high-temperature gate valve I402 is opened, and the amount of the high-temperature active raw material taken out from the discharge pipe of the cyclone 102 of the last-stage kiln tail preheater can be regulated and controlled by controlling the rotating speed of the high-temperature rotary discharger 403. The material taking amount can be freely controlled according to the requirement, and the operation is simple and convenient.
The cooling means of the cooling unit 20 is air cooling to lower the temperature of the high temperature active raw meal taken out from the decomposition unit.
In order to ensure that the taken high-temperature active raw material can be cooled to the required temperature, an air-cooled cooling unit is adopted for two-stage suspension cooling.
Referring to fig. 2, the cooling unit 20 includes a first stage cyclone 201 and a second stage cyclone 202, the other end of the material separating pipe 401 of the material taking unit is connected to an outlet air pipe of the first stage cyclone 201, the outlet air pipe of the first stage cyclone is connected to an inlet of the second stage cyclone 202, a discharging pipe of the second stage cyclone 202 is connected to an inlet of the first stage cyclone 201, cooling air is introduced into the inlet of the first stage cyclone 201, and an outlet air pipe of the second stage cyclone 202 is connected to the exhaust gas treatment system 204 through a fan 203. The working principle of the technical scheme is as follows: the high-temperature active raw materials taken out from the material taking unit firstly enter the outlet air pipe of the first-stage cyclone 201 and then enter the second-stage cyclone 202, most of the active raw materials are collected under the separation action of the second-stage cyclone 202, and the second-stage cyclone 202 preferably adopts a cyclone with the separation efficiency of more than 90%. The temperature of the active raw material collected from the second-stage cyclone 202 is 300-600 ℃, the active raw material is mixed with cooling air and enters the first-stage cyclone 201, the first-stage cyclone preferably adopts a cyclone with the separation efficiency of more than 80%, and the temperature of the active raw material separated by the first-stage cyclone 201 is reduced to below 150 ℃. Under the induced air of the fan 203, the cooling air firstly passes through the first-stage cyclone 201 from bottom to top and then passes through the second-stage cyclone 202, the dust-containing air which is discharged from the second-stage cyclone 202 enters the cement kiln flue gas and waste gas treatment system 204 after passing through the fan 203, and the waste gas treatment system 204 adopts the existing waste gas treatment device, such as a bag-type dust collector. The high-temperature active raw material can be cooled to below 150 ℃ after being subjected to two-stage suspension cooling, the feasibility of a scheme for directly taking the high-temperature active raw material is realized, and the cooling efficiency is high.
Referring to fig. 2, the discharge pipe of the second stage cyclone 202 is further connected to a material distribution pipe located at the upper part of the first high temperature gate valve 402, and the discharge pipe of the second stage cyclone 202 is provided with a material distribution valve 205 at a branch. The temperature of the active raw materials collected from the second-stage cyclone 202 is 300-600 ℃, the active raw materials are divided into two parts through the material dividing valve 205, one part of the active raw materials is mixed with the high-temperature active raw materials with the temperature of 800-950 ℃ in the material taking pipe 401, the temperature of the high-temperature active raw materials is reduced, the temperature of the mixed materials entering the high-temperature rotary discharger 403 is enabled to be lower than 700 ℃, and therefore the requirement on high-temperature resistant materials of the high-temperature rotary discharger 403 is reduced. Mixing a part of the active raw material from the second stage cyclone 202 with the high temperature active raw material just taken out can reduce the temperature of the mixed material to be more than 700 ℃, thereby protecting the high temperature material rotary discharger.
Referring to fig. 2, a discharge port of the first stage cyclone 201 is connected to a collecting bin 206, a discharge port of the collecting bin 206 is provided with a first gate valve 207 and a screw feeder 208 with a meter, and an outlet of the screw feeder 208 with the meter is connected to the digestion unit 30. The cooled active raw materials are firstly fed into a material collecting bin 206 before digestion and synergism, and are fed into the digestion unit 30 after being measured by a screw feeder 208 with a meter, and the storage period of the material collecting bin 206 is less than 24 hours so as to avoid raw material hardening. The feeding speed and the feeding amount are controlled by the spiral feeder with the meter, and the operation is convenient.
The digestion mode of the digestion unit 30 is dry digestion. In practice, the digestion unit 30 may be implemented as an existing dry digester. By spraying water into the digestion unit 30, the calcium oxide in the material reacts with water to generate active calcium hydroxide, and the material exiting the digestion unit 30 is an active desulfurizer. The independent dry digester is adopted, so that the digestibility of calcium oxide can reach over 90 percent, and the activity of the prepared desulfurizer is higher.
Referring to fig. 2, the exhaust port of the digestion unit 30 is connected to a cement kiln flue gas and exhaust gas treatment system 204 through an air duct of the cooling unit 20. In specific implementation, the exhaust port of the digestion unit 30 may be connected to the outlet air duct of the first stage cyclone 201 of the cooling unit 20 through an exhaust duct, or may be connected to the outlet air duct of the second stage cyclone 202 of the cooling unit 20, and further connected to the flue gas and exhaust gas treatment system 204 of the cement kiln. The dusty water vapor out of the digestion unit 30 enters the two-stage suspension cooling unit 20 through the exhaust pipeline and finally enters the waste gas treatment system 204, the dusty water vapor is purified through the waste gas treatment system 204, the atmospheric pollution is avoided, a dusty water vapor purification treatment device does not need to be arranged independently, and the investment and the operation cost are saved.
Referring to fig. 2, the digestion unit 30, the desulfurizing agent delivery unit 60 and the kiln tail preheater are connected in sequence. The desulfurizer conveying unit 60 comprises a roots blower 601, a desulfurizer bin 602, a gate valve II 605, a rotary feeder 606, a conveying chute 603 and a lifter 604 which are connected in sequence through a conveying pipeline, a discharge port of the digestion unit 30 is connected with the conveying pipeline between the roots blower 601 and the desulfurizer bin 602, and desulfurizer discharged by the lifter 604 is fed into a kiln tail preheater. Under the power of the Roots blower 601, air is used as a pneumatic transmission medium to transmit the desulfurizer discharged from the digestion unit 30 into a desulfurizer bin 602, a gate valve II 605 and a rotary feeder 606 are arranged at a discharge port of the desulfurizer bin 602 and are used for adjusting discharge capacity, the desulfurizer is fed into the kiln tail preheater through a conveying chute 603, a lifter 604 and a conveying chute 607, and during specific implementation, the desulfurizer can be fed into a pipeline between a cyclone cylinder of the first-stage kiln tail preheater and a cyclone cylinder of the second-stage kiln tail preheater, and in the pipeline, the desulfurizer reacts with kiln tail flue gas to remove SO in the flue gas2Thereby reducing SO in the tail flue gas of the kiln2And (4) content.
When the sulfur content in the feedstock is low, e.g. flue gas SO2Background concentration below 500mg/Nm3And in time, the corresponding desulfurization efficiency of the dry desulfurization system can meet the environmental protection emission standard of the cement industry. At this time, from the viewpoint of economical operation cost, the dry desulfurization system can be adopted to ensure that the cement clinker production system continues to operate and meet the requirement of flue gas SO2And (4) emission standard.
To sum up, the utility model discloses a cement kiln deals with the technique in coordination and establishes cement clinker production line calcium circulation dry desulfurization system, adopts the self-control hot raw material of cement kiln, and in the active raw material after cooling, digestion was as the desulfurizer through desulfurizer conveying unit 60 feeding kiln tail preheater, the active raw material after the digestion reacted as desulfurizer and kiln tail flue gas, and SO in the desorption flue gas2Thereby reducing SO in the tail flue gas of the kiln2Content, utilizing the self-characteristics of kiln system to solve the problem of smoke gas dioxygenSulfur sulfide discharge, thereby partially or completely replacing the purchased desulfurizing agent, saving the cost of the purchased desulfurizing agent and reducing the resource consumption of the limestone mine.
Example 2
In contrast to example 1, the active hot raw meal is taken out of the outlet ductwork of the decomposing furnace 101.
Referring to fig. 3 and 4, the cooling unit 20 is connected to an outlet air duct of the decomposing furnace 101 through a material taking unit. The active raw material out of the decomposing furnace enters the cyclone 102 of the last-stage kiln tail preheater along with most of the flue gas, and the rest enters the cooling unit 20 for cooling through the material taking unit.
The material taking unit comprises a material taking cyclone barrel 404, a high-temperature gate valve II 405 is arranged on an inlet pipeline of the material taking cyclone barrel 404, and a high-temperature gate valve III 406 is arranged on an outlet air pipe of the material taking cyclone barrel 404; an inlet pipeline of the material taking cyclone cylinder 404 is connected with an outlet air pipe of the decomposing furnace 101, an outlet air pipe of the material taking cyclone cylinder 404 is connected with an outlet air pipe of a last-stage or a penultimate kiln tail preheater, and a discharging pipe of the material taking cyclone cylinder 404 is connected with the cooling unit 20.
When material is required to be taken, the material amount entering the material taking cyclone barrel 404 is adjusted through the opening degrees of the high-temperature gate valve II 405 and the high-temperature gate valve III 406. The material taking amount can be freely controlled according to the requirement, and the operation is simple and convenient. Under the separating action of the material-taking cyclone cylinder 404, the air out of the material-taking cyclone cylinder 404 enters the inlet air pipe of the penultimate kiln tail preheater cyclone cylinder 103 or the penultimate kiln tail preheater cyclone cylinder 104, the high-temperature air returns to the heat exchange pipeline of the kiln tail preheater, most heat is recovered, the influence on the energy consumption of the system is small, and the material out of the material-taking cyclone cylinder 404 enters the cooling unit 20. FIG. 3 shows the entry of air out of the extraction cyclone 404 into the penultimate kiln tail preheater cyclone 103, and FIG. 4 shows the entry of air out of the extraction cyclone 404 into the penultimate kiln tail preheater cyclone 104.
The discharge pipe of the material taking cyclone 404 of the material taking unit is connected with the outlet air pipe of the first stage cyclone 201 of the cooling unit 20. The high-temperature active raw material taken out from the discharge pipe of the material taking cyclone 404 enters the outlet air pipe of the first stage cyclone 201 first, so that the taken-out high-temperature active raw material is fully cooled.
Example 3
Different from the embodiment 1 and the embodiment 2, referring to fig. 5, the digestion unit 30 is further provided with a quicklime feeding port 301. When equipment maintenance or system failure or SO in flue gas is carried out2When the concentration is high or the self-made desulfurizer made of active raw materials cannot meet the self-sufficient desulfurization requirement of the system, a certain amount of quicklime can be added into the digestion unit 30 except for the active raw materials, so that the desulfurization work is stably carried out, and the high-efficiency desulfurization is realized.
Example 4
Different from the embodiments 1, 2 and 3, referring to fig. 6, the desulfurizing agent bin 602 is further provided with an external desulfurizing agent charging port 608. When equipment maintenance or system failure or SO in flue gas is carried out2When the concentration is high or the self-made desulfurizer of the active raw material can not meet the self-sufficient desulfurization requirement of the system, a certain amount of purchased desulfurizer can be added into the desulfurizer entering the kiln tail preheater besides the self-made desulfurizer of the active raw material, so that the stable operation of desulfurization is ensured, and the high-efficiency desulfurization is realized.
Claims (10)
1. A calcium circulation dry desulphurization system of a cement clinker production line comprises a decomposition unit (10) for decomposing raw materials into active hot raw materials, wherein the decomposition unit (10) comprises a plurality of stages of kiln tail preheaters and a decomposition furnace (101); the device is characterized by also comprising a desulfurizer preparation unit and a desulfurizer conveying unit (60); the desulfurizer preparation unit comprises a cooling unit (20) connected with a discharge port of the decomposition unit (10), and a digestion unit (30) connected with a discharge port of the cooling unit (20); and a discharge hole of the digestion unit (30) is connected with a desulfurizer conveying unit (60), and the desulfurizer conveying unit (60) is connected with a kiln tail preheater.
2. The calcium circulation dry desulphurization system of the cement clinker production line according to claim 1, wherein the cooling unit (20) is connected with a discharge pipe of a cyclone (102) of a final-stage kiln tail preheater through a material taking unit; the material taking unit comprises a material distributing pipe (401), a high-temperature gate valve I (402) and a high-temperature rotary discharger (403), wherein the high-temperature gate valve I (402) is arranged on the material distributing pipe, one end of the material distributing pipe (401) is connected with a material discharging pipe of a cyclone cylinder (102) of a last-stage kiln tail preheater, and the other end of the material distributing pipe is connected with the cooling unit (20).
3. The calcium circulation dry desulphurization system of the cement clinker production line as recited in claim 1, wherein the cooling unit (20) is connected with the outlet air duct of the decomposing furnace (101) through a material taking unit; the material taking unit comprises a material taking cyclone cylinder (404), a high-temperature gate valve II (405) is arranged on an inlet pipeline of the material taking cyclone cylinder (404), and a high-temperature gate valve III (406) is arranged on an outlet air pipe of the material taking cyclone cylinder (404); an inlet pipeline of the material taking cyclone (404) is connected with an outlet air pipe of the decomposing furnace (101), an outlet air pipe of the material taking cyclone (404) is connected with an outlet air pipe of a last-stage or penultimate kiln tail preheater, and a discharging pipe of the material taking cyclone (404) is connected with the cooling unit (20).
4. The cement clinker production line calcium circulation dry desulphurization system of any one of claims 1 to 3, wherein the cooling unit is a two-stage suspension cooling.
5. The calcium circulation dry desulphurization system of the cement clinker production line as recited in claim 2, wherein the cooling unit (20) comprises a first stage cyclone (201) and a second stage cyclone (202), the other end of the material separating pipe (401) of the material taking unit is connected with the outlet air pipe of the first stage cyclone (201), the outlet air pipe of the first stage cyclone (201) is connected with the inlet of the second stage cyclone (202), the discharging pipe of the second stage cyclone (202) is connected with the inlet of the first stage cyclone (201), the inlet of the first stage cyclone (201) is fed with cooling air, and the outlet air pipe of the second stage cyclone (202) is connected with the waste gas treatment system (204) through the fan (203); the feeding pipe of the second-stage cyclone cylinder (202) is also connected with a material distribution pipe positioned at the upper part of the high-temperature gate valve I (402), and the feeding pipe of the second-stage cyclone cylinder (202) is provided with a material distribution valve (205) at a branch position.
6. The calcium circulation dry desulphurization system of the cement clinker production line as recited in claim 3, wherein the cooling unit (20) comprises a first stage cyclone (201) and a second stage cyclone (202), the unloading pipe of the material-taking cyclone (404) of the material-taking unit is connected with the outlet air pipe of the first stage cyclone (201), the outlet air pipe of the first stage cyclone (201) is connected with the inlet of the second stage cyclone (202), the unloading pipe of the second stage cyclone (202) is connected with the inlet of the first stage cyclone (201), the inlet of the first stage cyclone (201) is fed with cooling air, and the outlet air pipe of the second stage cyclone (202) is connected with the waste gas treatment system (204) through the fan (203).
7. The calcium circulation dry desulphurization system of the cement clinker production line according to claim 5 or 6, wherein the discharge opening of the first stage cyclone (201) is connected with a collecting bin (206) through a discharge pipe, the discharge opening of the collecting bin (206) is provided with a first gate valve (207) and a screw feeder (208) with a meter, and the outlet of the screw feeder (208) with the meter is connected with the digestion unit (30).
8. The cement clinker production line calcium circulation dry desulphurization system of claim 5 or 6, wherein the digestion mode of the digestion unit (30) is dry digestion; the exhaust port of the digestion unit (30) is connected with an exhaust gas treatment system (204) through an air pipe of the cooling unit (20).
9. The cement clinker production line calcium circulation dry desulphurization system of claim 1, wherein the slaking unit (30) is further provided with a quicklime feed inlet (301).
10. The cement clinker production line calcium circulation dry desulphurization system as claimed in claim 1, wherein the desulfurizer conveying unit (60) comprises a roots blower (601), a desulfurizer bin (602), a gate valve two (605), a rotary feeder (606), a conveying chute (603) and a lifter (604) which are connected in sequence through a conveying pipeline, a discharge port of the digestion unit (30) is connected with the conveying pipeline between the roots blower (601) and the desulfurizer bin (602), and the desulfurizer discharged by the lifter (604) is fed into a kiln tail preheater.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110052158A (en) * | 2019-06-06 | 2019-07-26 | 天津水泥工业设计研究院有限公司 | One kind recycling dry method desulfuration system based on cement clinker production line calcium |
| CN115430272A (en) * | 2022-10-24 | 2022-12-06 | 北京北科环境工程有限公司 | Preparation method of calcium-based SDS (sodium dodecyl sulfate) desulfurization process raw material |
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2019
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110052158A (en) * | 2019-06-06 | 2019-07-26 | 天津水泥工业设计研究院有限公司 | One kind recycling dry method desulfuration system based on cement clinker production line calcium |
| CN110052158B (en) * | 2019-06-06 | 2023-12-22 | 天津水泥工业设计研究院有限公司 | Calcium circulation dry desulfurization system based on cement clinker production line |
| CN115430272A (en) * | 2022-10-24 | 2022-12-06 | 北京北科环境工程有限公司 | Preparation method of calcium-based SDS (sodium dodecyl sulfate) desulfurization process raw material |
| CN115430272B (en) * | 2022-10-24 | 2023-07-25 | 北京北科环境工程有限公司 | Preparation method of calcium-based SDS desulfurization process raw material |
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