Cement kiln system dechlorination and chlorine ash resource utilization method

Abstract

The invention discloses a method for dechlorination and chlorine ash resource utilization of a cement kiln system. The method comprises the following steps: step 1, extracting waste gas of a smoke chamber at the tail of a kiln to shock cooling equipment, and separating the cooled waste gas through cyclone separation equipment; 2, the waste gas enters a rotary heat exchange device; 3, the waste gas exhausted by the rotary heat exchange device communicates with a gas-water mixing system, and dust in the waste gas is mixed with water in the gas-water mixing system to form slurry; 4, when the concentration of the slurry at the bottom of the gas-water mixing system reaches a set standard, a slurry pump is started to convey the slurry to a chlorine ash utilization system; step 5, carrying out solid-liquid separation on the slurry by the chlorine ash utilization system, and conveying the separated solid to the rotary heat exchanger in the step 2 for drying; the separated liquid enters a potassium salt and sodium salt production system; and step 6, filtering and distilling the liquid by the potassium salt and sodium salt production system to separate out potassium salt and sodium salt. According to the method, the waste heat of the waste gas can be effectively utilized, and meanwhile potassium salt and sodium salt in the chlorine ash can be recycled.

Description

Technical Field

[0001] The invention relates to a dechlorination system, in particular to a method for dechlorination of a cement kiln system and resource utilization of chlorine ash. Background Art

[0002] Raw materials such as limestone, sandstone, shale, and iron are mixed in a certain proportion, ground, and then calcined at high temperature to produce cement clinker. Limestone, sandstone, shale, iron and other raw materials are all from nature, and they all contain chloride ions in different proportions, which will solidify in the clinker during the calcination process. However, chloride ions are strong acid radicals with strong corrosiveness. In the process of making reinforced concrete, they are easy to react with the alkaline substances produced by the hydration of steel bars and clinker, affecting the temperature resistance of concrete, thereby affecting the safety of the entire building.

[0003] Therefore, in the process of cement clinker production, the chloride ion content needs to be strictly controlled, generally controlled below 0.06%. If it exceeds, it will cause serious crusting in the system, unqualified clinker quality and other problems. Therefore, it is necessary to set up a dechlorination system in the clinker production process to discharge chloride ions from the burning system.

[0004] The existing dechlorination system generally sets an air intake in the smoke chamber to extract the flue gas in the smoke chamber. The flue gas is cooled to reduce its temperature to below 400°C. At this temperature, the chloride ions in the flue gas crystallize. The coarse particles produced by the crystallization are collected by collecting dust from the low-temperature flue gas. Since the coarse particles have a small specific surface area and relatively fewer chloride ions are attached, these coarse particles can be returned to the decomposition furnace, while fine particles and smoke ash with more chloride ions enter the air cooler with the exhaust gas to be cooled to less than 200°C, and then discharged from the system through the dust collector and the fan.

[0005] The temperature of the exhaust gas discharged by the existing technical solution is still very high, which will cause a waste of kinetic energy, and the collected dechlorination ash contains about 20% potassium chloride. The existing technology is only used as a cement admixture, and the level of resource utilization is low. Summary of the invention

[0006] The purpose of the present invention is to provide a method for dechlorination and resource utilization of chlorine ash in a cement kiln system, which can effectively utilize the waste heat of exhaust gas and also recover potassium salt and sodium salt in the chlorine ash.

[0007] In order to achieve the above-mentioned object, the present invention provides a method for dechlorination and resource utilization of chlorine ash in a cement kiln system, and the method for dechlorination and resource utilization of chlorine ash in a cement kiln system comprises:

[0008] Step 1, extracting the exhaust gas from the kiln tail smoke chamber to a quenching device, wherein the temperature of the exhaust gas after being cooled by the quenching device is not higher than 400°C, and the cooled exhaust gas is separated by a cyclone separation device, and the exhaust gas with high chlorine content is input to the next process;

[0009] Step 2: the exhaust gas discharged from the cyclone separator in step 1 enters the rotary heat exchange device;

[0010] Step 3: In step 2, the exhaust gas discharged from the rotary heat exchange device is connected to the gas-water mixing system, and the dust in the exhaust gas is mixed with water in the gas-water mixing system to form a slurry;

[0011] Step 4: When the slurry concentration at the bottom of the gas-water mixing system in step 3 reaches the set standard, the slurry pump is started to transport the slurry to the chlorine ash utilization system;

[0012] Step 5: The chlorine ash utilization system performs solid-liquid separation on the slurry delivered by the slurry pump in step 4, and the separated solid is delivered to the rotary heat exchanger in step 2 for drying; the separated liquid enters the potassium salt and sodium salt production system;

[0013] Step 6: Potassium salt and sodium salt production system: Filter and distill the liquid separated in step 5 to separate potassium salt and sodium salt.

[0014] Preferably, the rotary heat exchange device in step 2 comprises a device body, a high-temperature pipe, a material inlet and a material outlet, wherein the material inlet and the material outlet are respectively located at the upper end and the lower end of the heat exchange device body, the high-temperature pipe is arranged in a flat shape, the flat high-temperature pipe is arranged in the device body, and the flat high-temperature pipe spirally extends from the lower end of the heat exchange device body to the upper end of the heat exchange device body;

[0015] The exhaust gas in step 2 enters the high-temperature pipe inlet at the lower end and flows out from the high-temperature pipe outlet at the upper end;

[0016] The solid in step 5 enters the material inlet at the upper end and flows out from the material outlet at the lower end.

[0017] Preferably, the rotary heat exchange device further comprises a water vapor collecting pipe, one end of which is in communication with the top of the heat exchange device body, and the other end of which is in communication with the high-temperature pipe outlet.

[0018] Preferably, in step 3, the gas-water mixing system includes a mixer shell, a spray device and a circulating slurry device located inside the shell, the spray device is arranged on the upper part of the shell, the circulating slurry device is arranged directly below the spray device to receive the liquid sprayed by the spray device, and an agitator is arranged inside the circulating slurry device.

[0019] Preferably, a circulation pipeline connected to the spraying device is provided on the upper part of the circulating slurry device.

[0020] Preferably, the gas-water mixing system further comprises a demisting device, and the demisting device is arranged on the top of the mixer housing and above the spraying device.

[0021] Preferably, a slurry concentration detector is provided in the circulating slurry device, and the slurry concentration detector is electrically connected to the slurry pump for starting the slurry pump.

[0022] Preferably, in step 5, the chlorine ash utilization system includes a centrifugal solid-liquid separator, the slurry is subjected to solid-liquid separation by the centrifugal solid-liquid separator, and the liquid separated by the centrifugal solid-liquid separator is transported to the potassium salt and sodium salt production system.

[0023] Preferably, the chlorine ash utilization system also includes a vacuum belt conveyor, and the solids separated by the centrifugal solid-liquid separator are transported to the vacuum belt conveyor. A liquid outlet is provided at the bottom of the vacuum belt conveyor, and the liquid outlet is connected to the potassium salt and sodium salt production system.

[0024] According to the above technical scheme, the waste gas extracted from the kiln tail smoke chamber of the present invention is cooled to below 400°C by a quenching device, and the chloride ions in the waste gas are condensed and crystallized. The coarse particles with a larger specific surface area have relatively fewer chloride ions attached, while the fine particles with a larger specific surface area have more chloride ions attached. Therefore, the cooled waste gas is separated into coarse particles by a cyclone separation device. Since the content of chloride ions in the coarse particles is relatively small, the coarse particles obtained at the discharge port of the separator can be sent back to the decomposition furnace. The fine particles and flue gas are sent to the rotary heat exchange device in the step from the exhaust port of the separator.

[0025] The temperature of the waste gas output from the separator exhaust port is still relatively high, and it can be used as a high-temperature medium in the rotary heat exchange device to heat and dry the material. The separator exhaust port is connected to the high-temperature pipe inlet, and the high-temperature gas enters the high-temperature pipe and flows out to the gas-water mixing system through the high-temperature pipe outlet. In the rotary heat exchange device, the waste gas is used as a high-temperature medium to heat and dry the solids separated from the slurry, so that these dried solids can be used as raw mill ingredients.

[0026] Therefore, by providing the rotary heat exchange device, the heat energy of the exhaust gas extracted from the smoke chamber can be fully utilized to avoid energy waste.

[0027] The spray device of the gas-water mixing system sprays water on the exhaust gas. The solid particles in the exhaust gas adhere to the water mist and fall into the circulating slurry device below. As more and more exhaust gas enters the gas-water mixing system, the slurry concentration in the circulating slurry device becomes higher and higher. When the slurry concentration reaches the set standard value, the slurry pump starts to transport the slurry to the chlorine ash utilization system.

[0028] The chlorine ash utilizes the system to separate the slurry into solids and liquids. The separated solids will be transported to the rotary heat exchange device as the dried material. These solids enter the device body through the material inlet. As the solids spiral down along the high-temperature pipeline, the heat exchange between the solids and the high-temperature exhaust gas continues. The temperature of the solids becomes higher and higher, and the water in them turns into water vapor and leaves the solids. When the solids reach the material outlet, these dried solids will be used as raw mill ingredients. The liquid separated from the slurry contains potassium salt and sodium salt, so these liquids can be transported to the potassium salt and sodium salt production system, and separated by filtration and distillation to reuse them as production materials.

[0029] Therefore, the method for removing chlorine from the cement kiln system and recycling chlorine ash can make full use of the thermal energy of the exhaust gas extracted from the smoke chamber by using the rotary heat exchange device 3, thereby avoiding energy waste. At the same time, the potassium salt and sodium salt in the exhaust gas can be recycled through the chlorine ash utilization system and the potassium salt and sodium salt production system.

[0030] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present invention but do not constitute a limitation of the present invention. In the accompanying drawings:

[0032] Figure 1 It is a work flow chart of the method for dechlorination and resource utilization of chlorine ash in cement kiln system;

[0033] Figure 2 It is a schematic diagram of a cyclone separation device.

[0034] Description of Reference Numerals

[0035] 1Quenching equipment72Nanofiltration

[0036] 2 cyclone separation equipment 21 separator outlet

[0037] 22 separator exhaust port 23 separator inlet

[0038] 3 Rotary heat exchange device 31 Device body

[0039] 32 High temperature pipeline 33 Material inlet

[0040] 34 Material outlet 35 High temperature pipeline inlet

[0041] 36 High temperature pipeline outlet 37 Water vapor collection pipe

[0042] 41 mixer housing 42 spray device

[0043] 43 Circulating slurry device 44 Circulating pipeline

[0044] 45 Demisting device 5 Centrifugal solid-liquid separator

[0045] 6 Vacuum belt conveyor 61 liquid outlet

[0046] 10 decomposition furnace 38 exhaust fan

[0047] 71 Crystallizer 73 Ultrafiltration DETAILED DESCRIPTION

[0048] The specific implementation of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the present invention, and is not used to limit the present invention.

[0049] In the present invention, unless otherwise specified, directional words contained in terms such as "above, top, directly below, upper end, lower end" merely represent the orientation of the term in normal usage, or are common names understood by those skilled in the art, and should not be regarded as limitations on the term.

[0050] like Figure 1 The method for dechlorination and resource utilization of chlorine ash in a cement kiln system comprises:

[0051] Step 1, extracting the exhaust gas from the kiln tail smoke chamber to the quenching device 1, the exhaust gas temperature after being cooled by the quenching device 1 is not higher than 400°C, the cooled exhaust gas is separated by the cyclone separation device 2, and the exhaust gas with high chlorine content is input to the next process;

[0052] Step 2: The exhaust gas discharged from the cyclone separator in step 1 enters the rotary heat exchange device 3;

[0053] In step 3 and step 2, the exhaust gas discharged from the rotary heat exchange device 3 is connected to the gas-water mixing system, and the dust in the exhaust gas is mixed with water in the gas-water mixing system to form a slurry;

[0054] Step 4: When the slurry concentration at the bottom of the gas-water mixing system in step 3 reaches the set standard, the slurry pump is started to transport the slurry to the chlorine ash utilization system;

[0055] Step 5: The chlorine ash utilization system performs solid-liquid separation on the slurry delivered by the slurry pump in step 4, and the separated solid is delivered to the rotary heat exchanger in step 2 for drying; the separated liquid enters the potassium salt and sodium salt production system;

[0056] Step 6: Potassium salt and sodium salt production system: Filter and distill the liquid separated in step 5 to separate potassium salt and sodium salt.

[0057] Through the implementation of the above technical solution, the exhaust gas extracted from the kiln tail smoke chamber is cooled to below 400°C by the quenching equipment, and the chloride ions in the exhaust gas are condensed and crystallized. The coarse particles with a larger specific surface area have relatively fewer chloride ions attached, while the fine particles with a larger specific surface area have more chloride ions attached. Therefore, the cooled exhaust gas is separated into coarse particles by the cyclone separation device 2. Since the content of chloride ions in the coarse particles is relatively small, the coarse particles obtained at the separator discharge port 21 can be sent back to the decomposition furnace. The fine particles and the flue gas are sent to the rotary heat exchange device 3 in step 2 from the separator exhaust port 22.

[0058] The temperature of the waste gas output from the separator exhaust port 22 is still relatively high, and can be used as a high-temperature medium of the rotary heat exchange device 3 to heat and dry the material. The separator exhaust port 22 is connected to the high-temperature pipe inlet 35, and the high-temperature gas enters the high-temperature pipe 32 and flows out to the gas-water mixing system through the high-temperature pipe outlet 36. In the rotary heat exchange device 3, the waste gas is used as a high-temperature medium to heat and dry the solids separated from the slurry, so that these dried solids can be used as raw mill ingredients.

[0059] Therefore, by providing the rotary heat exchange device 3, the heat energy of the exhaust gas extracted from the smoke chamber can be fully utilized to avoid energy waste.

[0060] The spray device 42 of the gas-water mixing system sprays water on the exhaust gas, and the solid particles in the exhaust gas adhere to the water mist and fall into the circulating slurry device 43 below. As more and more exhaust gas enters the gas-water mixing system, the slurry concentration in the circulating slurry device 43 becomes higher and higher. When the slurry concentration reaches the set standard value, the slurry pump starts to transport the slurry to the chlorine ash utilization system.

[0061] The chlorine ash utilization system separates the slurry into solids and liquids, and the separated solids are transported to the rotary heat exchange device 3 as dried materials. These solids enter the device body 31 through the material inlet 33. In the process of the solid spirally descending along the high-temperature pipe 32, the heat exchange between the solid and the high-temperature exhaust gas is also continuously carried out. The temperature of the solid is getting higher and higher, and the water in it will turn into water vapor and leave the solid. When the solid reaches the material outlet 34, these dried solids will be used as raw material mill ingredients. The liquid separated from the slurry contains potassium salt and sodium salt, so these liquids can be transported to the potassium salt and sodium salt production system, and separated by filtration and distillation to use as production materials.

[0062] Therefore, the method for removing chlorine from the cement kiln system and recycling chlorine ash can make full use of the thermal energy of the exhaust gas extracted from the smoke chamber by using the rotary heat exchange device 3, thereby avoiding energy waste. At the same time, the potassium salt and sodium salt in the exhaust gas can be recycled through the chlorine ash utilization system and the potassium salt and sodium salt production system.

[0063] In this embodiment, preferably, the rotary heat exchange device 3 in step 2 includes a device body 31, a high-temperature pipe 32, a material inlet 33 and a material outlet 34, wherein the material inlet 33 and the material outlet 34 are respectively located at the upper end and the lower end of the heat exchange device body 31, and the high-temperature pipe 32 is configured to be flat, and the flat high-temperature pipe 32 is disposed in the device body 31, and the flat high-temperature pipe 32 spirally extends from the lower end of the heat exchange device body 31 to the upper end of the heat exchange device body 31;

[0064] The exhaust gas in step 2 enters the high-temperature pipe inlet 35 at the lower end and flows out from the high-temperature pipe outlet 36 at the upper end;

[0065] The solid in step 5 enters the material inlet 33 at the upper end and flows out from the material outlet 34 at the lower end.

[0066] The temperature of the exhaust gas discharged from the separator exhaust port 22 is about 400°C. These gases are input into the high-temperature pipe inlet 35 of the rotary heat exchange device 3 as high-temperature media. These high-temperature gases spirally rise in the high-temperature pipe 32 and simultaneously exchange heat with the solids spirally descending along the upper surface of the high-temperature pipe 32. The solids are dried during the heat exchange process, thereby realizing the effective utilization of the thermal energy of these high-temperature gases.

[0067] In this embodiment, preferably, the rotary heat exchange device 3 further includes a water vapor collecting pipe 37 , one end of which is connected to the top of the heat exchange device body 31 , and the other end of which is connected to the high-temperature pipe outlet 36 .

[0068] The high-temperature pipe inlet 35 is arranged at the lower end of the device body 31, and the high-temperature pipe outlet 36 is arranged at the upper end of the device body 31. An exhaust fan 38 is also arranged on the high-temperature pipe outlet 36. The exhaust fan 38 provides negative pressure for the system, so that the exhaust gas in the entire exhaust gas conveying system can always have the power to flow.

[0069] The solid is heated and dried in the rotary heat exchange device 3, and the water therein evaporates into water vapor and rises to the top of the device body 31. A water vapor collecting pipe 37 is arranged on the top of the device body 31 to collect the water vapor. After the water vapor is collected, it is transported to the high-temperature pipe outlet 36 through the water vapor collecting pipe 37. In the high-temperature pipe outlet 36, the water vapor and the exhaust gas are preliminarily mixed to achieve preliminary water-gas mixing.

[0070] In this embodiment, preferably, in step 3, the gas-water mixing system includes a mixer shell 41, a spray device 42 and a circulating slurry device 43 located inside the shell, the spray device 42 is arranged at the upper part of the shell, the circulating slurry device 43 is arranged directly below the spray device 42 to receive the liquid sprayed by the spray device 42, and an agitator is arranged inside the circulating slurry device 43.

[0071] The exhaust fan 38 finally transports the exhaust gas to the gas-water mixing system. The mixer shell 41 is configured to be sealed, and the exhaust gas is input between the spray device 42 and the circulating slurry device 43. The upper spray device 42 continuously sprays water mist, which adheres to fine particles, dust, etc. in the exhaust gas. At the same time, since the exhaust gas loses power after entering the mixer shell 41, the solid particles in the exhaust gas will fall into the circulating slurry device 43 below, and are fully mixed with water in the circulating slurry device 43, and form slurry under the action of the agitator.

[0072] In this embodiment, preferably, a circulation pipeline 44 connected to the spraying device 42 is provided on the upper part of the circulating slurry device 43 .

[0073] In order to realize the recycling of water, a circulation pipeline 44 connected to the spraying device 42 is arranged on the upper part of the circulating slurry device 43. The liquid in the upper part of the circulating slurry device 43 enters the spraying device 42 through the circulation pipeline 44 and is sprayed into the mixer shell 41 again as the water source of the spraying device 42.

[0074] In this way, frequent addition of water to the gas-water mixing system can be avoided, thereby improving the efficiency of increasing the slurry concentration.

[0075] In this embodiment, preferably, the gas-water mixing system further includes a demisting device 45 , which is disposed on the top of the shell and above the spraying device 42 .

[0076] After the solid particles in the exhaust gas are collected by the spray device 42, the gas in the exhaust gas will rise to the top of the device body 31 and be discharged to the outside through the exhaust pipe at the top. Since there is still a large amount of water vapor in the mixer shell 41, a demisting device 45 is set on the top of the mixer shell 41. The demisting device 45 can effectively intercept the water vapor to avoid the waste of water resources caused by the outflow of a large amount of water vapor. At the same time, by intercepting the water vapor, it is also possible to avoid frequent replenishment of water in the gas-water mixing system.

[0077] In this embodiment, preferably, a slurry concentration detector is provided in the circulating slurry device 43, and the slurry concentration detector is electrically connected to the slurry pump for starting the slurry pump.

[0078] The slurry concentration detector mainly monitors the pH value of the slurry. Preferably, when the pH of the slurry reaches or even exceeds 6, the slurry pump can be started to pump the slurry in the circulating slurry device 43 to the chlorine ash utilization system.

[0079] In this embodiment, preferably, in step 5, the chlorine ash utilization system includes a centrifugal solid-liquid separator 5, the slurry is subjected to solid-liquid separation by the centrifugal solid-liquid separator 5, and the liquid separated by the centrifugal solid-liquid separator 5 is transported to the potassium salt and sodium salt production system.

[0080] In this embodiment, preferably, the chlorine ash utilization system also includes a vacuum belt conveyor 6, and the solid separated by the centrifugal solid-liquid separator 5 is transported to the vacuum belt conveyor 6. A liquid outlet 61 is provided at the lower part of the vacuum belt conveyor 6, and the liquid outlet 61 is connected to the potassium salt and sodium salt production system.

[0081] The solid separated by the centrifugal solid-liquid separator 5 still contains a small amount of liquid, so these solids are sent to the vacuum belt conveyor 6, and the liquid in the solid is collected again by the vacuum belt conveyor 6. The collected liquid is transported to the potassium salt and sodium salt production system.

[0082] The solids outputted by the vacuum belt conveyor 6 will be transported to the rotary heat exchange device 3 and dried in the rotary heat exchange device 3. The water in the solids will be further evaporated in the rotary heat exchange device 3, and the evaporated water will become water vapor and mix with the exhaust gas at the high-temperature pipe outlet 36 to achieve preliminary mixing of the water vapor and the exhaust gas. In the high-temperature pipe outlet 36, the water vapor will combine with the solid particles in the exhaust gas and condense into small water droplets, which is conducive to improving the separation of solids and gases in the gas-water mixing system.

[0083] The preferred embodiments of the present invention are described in detail above in conjunction with the accompanying drawings. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, a variety of simple modifications can be made to the technical solution of the present invention, and these simple modifications all belong to the protection scope of the present invention.

[0084] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0085] In addition, various embodiments of the present invention may be arbitrarily combined, and as long as they do not violate the concept of the present invention, they should also be regarded as the contents disclosed by the present invention.

Claims

1. A method for dechlorination and resource utilization of chlorine ash in a cement kiln system, characterized in that: The method for dechlorination and resource utilization of chlorine ash in a cement kiln system comprises: Step 1, extracting waste gas from the kiln tail smoke chamber to the quenching device (1), the temperature of the waste gas after cooling by the quenching device (1) is not higher than 400° C. The cooled waste gas is separated by the cyclone separation device (2), and the waste gas with high chlorine content is input to the next process; Step 2: the exhaust gas discharged from the cyclone separator in step 1 enters the rotary heat exchange device (3); In step 3 and step 2, the exhaust gas discharged from the rotary heat exchange device (3) is connected to the gas-water mixing system, and the dust in the exhaust gas is mixed with water in the gas-water mixing system to form a slurry; Step 4: When the slurry concentration at the bottom of the gas-water mixing system in step 3 reaches the set standard, the slurry pump is started to transport the slurry to the chlorine ash utilization system; Step 5: The chlorine ash utilization system performs solid-liquid separation on the slurry delivered by the slurry pump in step 4, and the separated solid is delivered to the rotary heat exchanger in step 2 for drying; the separated liquid enters the potassium salt and sodium salt production system; Step 6: Potassium salt and sodium salt production system: Filter and distill the liquid separated in step 5 to separate potassium salt and sodium salt.

2. The method for dechlorination and resource utilization of chlorine ash in a cement kiln system according to claim 1, characterized in that: The rotary heat exchange device (3) in step 2 comprises a device body (31), a high-temperature pipe (32), a material inlet (33) and a material outlet (34), wherein the material inlet (33) and the material outlet (34) are respectively located at the upper end and the lower end of the heat exchange device body (31), and the high-temperature pipe (32) is arranged in a flat shape, and the flat high-temperature pipe (32) is arranged in the device body (31), and the flat high-temperature pipe (32) spirally extends from the lower end of the heat exchange device body (31) to the upper end of the heat exchange device body (31); The exhaust gas in step 2 enters the high-temperature pipe inlet (35) at the lower end and flows out from the high-temperature pipe outlet (36) at the upper end; The solid in step 5 enters the material inlet (33) at the upper end and flows out from the material outlet (34) at the lower end.

3. The method for dechlorination and resource utilization of chlorine ash in a cement kiln system according to claim 2, characterized in that: The rotary heat exchange device (3) further comprises a water vapor collection pipe (37), one end of which is in communication with the top of the heat exchange device body (31), and the other end of which is in communication with the high-temperature pipe outlet (36).

4. The method for dechlorination and resource utilization of chlorine ash in a cement kiln system according to claim 1, characterized in that: In step 3, the gas-water mixing system includes a mixer shell (41), a spray device (42) and a circulating slurry device (43) located inside the shell, wherein the spray device (42) is arranged at the upper part of the shell, and the circulating slurry device (43) is arranged directly below the spray device (42) to receive the liquid sprayed by the spray device (42), and an agitator is arranged inside the circulating slurry device (43).

5. The method for dechlorination and resource utilization of chlorine ash in a cement kiln system according to claim 4, characterized in that: A circulation pipeline (44) connected to the spraying device (42) is arranged on the upper part of the circulating slurry device (43).

6. The method for dechlorination and resource utilization of chlorine ash in a cement kiln system according to claim 4, characterized in that: The gas-water mixing system further comprises a demisting device (45), wherein the demisting device (45) is arranged on the top of the mixer housing (41) and is located above the spraying device (42).

7. The method for dechlorination and resource utilization of chlorine ash in a cement kiln system according to claim 4, characterized in that: The circulating slurry device (43) is provided with a slurry concentration detector, which is electrically connected to the slurry pump and is used to start the slurry pump.

8. The method for dechlorination and resource utilization of chlorine ash in a cement kiln system according to claim 2, characterized in that: In step 5, the chlorine ash utilization system includes a centrifugal solid-liquid separator (5), the slurry is subjected to solid-liquid separation by the centrifugal solid-liquid separator (5), and the liquid separated by the centrifugal solid-liquid separator (5) is transported to the potassium salt and sodium salt production system.

9. The method for dechlorination and resource utilization of chlorine ash in a cement kiln system according to claim 8, characterized in that: The chlorine ash utilization system also includes a vacuum belt conveyor (6), and the solid separated by the centrifugal solid-liquid separator (5) is transported to the vacuum belt conveyor (6). A liquid outlet (61) is provided at the bottom of the vacuum belt conveyor (6), and the liquid outlet (61) is connected to the potassium salt and sodium salt production system.

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