CN114368922A

CN114368922A - Method for monitoring and disposing chlorine in cement clinker production system for cooperatively disposing waste incineration fly ash and cement clinker production system

Info

Publication number: CN114368922A
Application number: CN202011094660.2A
Authority: CN
Inventors: 杨李锋; 熊运贵; 张峰; 鲁皖; 梁红玉; 向薇; 冯庆云
Original assignee: Individual
Current assignee: Beijing Youjuyuan Environmental Protection Engineering Technology Co ltd
Priority date: 2020-10-14
Filing date: 2020-10-14
Publication date: 2022-04-19

Abstract

The invention discloses a method for monitoring and disposing chlorine in a cement clinker production system for cooperatively disposing waste incineration fly ash and a cement clinker production system thereof, belonging to the technical field of environmental protection. The provided chlorine monitoring and disposing method is based on a cement clinker production system, the chloride ion content of hot raw materials and the chloride ion content of cement clinker in a cement kiln system are respectively detected, and the chloride ion circulation rate in the cement kiln system is accurately controlled to be maintained within the range of 50-500 by adjusting and controlling the technological parameters of the cement kiln system and/or the air discharge amount of a bypass air discharge device, so that the good and stable running state of the cement kiln system can be ensured, the influence of chlorine elements on the yield and quality of the cement clinker is avoided, and a potassium chloride product with high economic value can be obtained.

Description

Method for monitoring and disposing chlorine in cement clinker production system for cooperatively disposing waste incineration fly ash and cement clinker production system

Technical Field

The invention belongs to the technical field of environmental protection, and particularly relates to a method for monitoring and disposing chlorine in a cement clinker production system for cooperatively disposing waste incineration fly ash and a cement clinker production system.

Background

The garbage incineration (or garbage incineration power generation) is a main mode for treating various municipal garbage, particularly domestic garbage, medical garbage, industrial garbage and other garbage. Because various wastes, especially medical wastes, contain a large amount of chlorine, which is a core element for generating dioxin (a kind of highly toxic substances), and particularly, dioxin is easily generated at the incineration temperature of 600-800 ℃, a large amount of dioxin belonging to a kind of highly toxic substances is contained in waste incineration fly ash. In addition, the waste incineration fly ash also contains various heavy metal substances. Therefore, it is necessary to safely dispose of the waste incineration fly ash.

At present, the disposal of the waste incineration fly ash mainly comprises solidification and stabilization technical chemical treatment methods, high-temperature disposal, safe landfill methods and the like, but the effect is not very ideal. Since dioxin is gradually reduced above 800 ℃, and the operating temperature of a cement kiln decomposition furnace is generally above 850 ℃, the cooperative disposal of waste incineration fly ash by a cement kiln is a new way of disposing fly ash that has been developed in recent years, and in brief, dioxin is decomposed by using high temperature of combustion in the process of calcining cement clinker, and fly ash waste is disposed in cooperation.

However, since the fly ash from waste incineration contains a large amount of chlorine elements (generally, the content is 6% to 12%), and in the production of cement clinker in the cement kiln, a certain amount of chlorine elements are generally contained in the calcination fuel (fire coal) and the production raw materials, when the fly ash from waste incineration is co-disposed in the cement kiln, these chlorine elements (existing as chloride ions) have serious negative effects on the clinker calcination process of the cement kiln, which may lead to the deterioration of the kiln conditions, and may cause process accidents such as skinning, blocking, rolling large balls, etc., which seriously affect the yield of cement clinker. And a large amount of chloride ions enter the cement clinker and then enter a cement product, so that the later hardness of the cement mortar is greatly inhibited, and the chloride ions can corrode building materials such as reinforcing steel bars and the like which are in contact with the cement mortar, so that the building quality is influenced. That is, the chloride ions also seriously affect the quality of the cement clinker.

Therefore, the current common practice is: the waste incineration fly ash is washed in advance, a large amount of chloride ions and soluble salts contained in the fly ash are removed by washing, and the residual low-chloride fly ash is sent to a cement kiln for disposal. Although the disposal method can technically solve the problem of co-disposing the chlorine element in the waste incineration fly ash by the cement kiln, the following problems also exist: firstly, the pretreatment and washing process of the fly ash is complex in process and high in treatment cost, small-batch treatment cannot be realized, and large-batch centralized treatment is required to improve the washing efficiency. For example, it is now generally efficient to build a fly ash water-wash pretreatment line that handles fly ash in 300 tons/day quantities. Secondly, the investment of a fly ash water washing pretreatment line is large. For example, the above-mentioned 300 ton/day fly ash water washing pretreatment line requires about 2 hundred million RMB investment in production equipment, without incurring land and personnel costs. Thirdly, the fly ash as hazardous waste is transported from each waste incineration plant (station) to the fly ash water-washing pretreatment plant and the low-chlorine fly ash after water-washing is transported again to the cement kiln, and the transportation volume is large. Specifically, about 1-1.2 kg of urban garbage is produced by each person per day, the fly ash generated by garbage incineration accounts for 3-5% of the weight of the original garbage, and a 300 ton/day fly ash water washing production line can cover 600 ten thousand of people by 1 kg and 5%. The method is more suitable compared with a large city, but the configuration is unreasonable for a small city and towns and villages with small population density. Fourth, because dioxin is a fat-soluble and water-insoluble toxic substance, the fly ash still contains a large amount of dioxin after washing with water, and the fly ash after washing with water is still a hazardous waste, and further disposal is still required according to the disposal requirements of the hazardous waste.

In the prior art, chlorine-containing flue gas generated in a cement kiln system is enriched by a bypass air release method and is removed from a production process by the bypass air release method. Specifically, chlorine element in ion form is combined with potassium element in cement production raw materials to generate potassium chloride microcrystal particles, and the potassium chloride microcrystal particles are enriched and captured in a bypass air release system by a cyclone separation device to form solid powder which is discharged from a cement kiln system. For example, when the concentration of the gas in the kiln is saturated as disclosed in CN101386481A, a high-concentration chlorine-containing flue gas is periodically released to the outside of the kiln by a simple bypass air release device, thereby reducing the concentration of chlorine in the kiln. However, the method only discharges a part of bypass air discharging ash in the kiln system in a rough discharging manner, and is specifically characterized in that the air discharging ash is periodically discharged only when chlorine-containing flue gas in the kiln system is saturated, and in addition, chlorine in fly ash also partially enters a burning zone kiln skin in the form of alkali chloride, so that the method has little effect from the viewpoint of inhibiting the influence of chlorine element on the yield and quality of cement clinker, and is specifically characterized in that the content of the chlorine element in cement kiln clinker products is still correspondingly increased and unstable, the chlorine element entering the burning zone kiln skin increases the thickness of the kiln skin, influences the rotation of the rotary kiln, the kiln skin falls off when the kiln skin is thickened to a certain degree, and the chlorine-containing kiln skin is also mixed into the cement clinker. Therefore, if such a method is used to obtain cement clinker satisfying the requirement of low chlorine content, the amount of fly ash from waste incineration must be reduced at each time, which significantly reduces the disposal efficiency of fly ash from waste incineration. And the content of chlorine element in the bypass air-bleed ash obtained by the method is low and unstable due to discontinuous discharge, and is generally less than 10%, and the content of converted potassium chloride is generally less than 20%. If the bypass air-bleed ash is to be utilized, for example, potassium chloride in the bypass air-bleed ash is extracted, because the content of the potassium chloride is low, the purification efficiency is low, and the method is not beneficial to industrial utilization. And the bypass air-released ash also contains a certain amount of harmful substances (the existing regulations manage according to hazardous wastes), cannot be buried according to common garbage, and is mostly accumulated and treated at present. There are also cases where a part is incorporated in the subsequent cement production, such as the method disclosed in the above-mentioned document CN101386481A, which adds chlorine again to the cement product, and still fails to completely solve the problem of high chlorine content in the cement, and the consumption amount added to the ground cement is limited. A typical dry-process kiln cement clinker production line with daily production of 5000 tons generally generates about 5-10 tons of bypass air-bleeding ash in one day, and because the treatment efficiency of the existing method is too low, the bypass air-bleeding ash occupies a large amount of space, thereby inhibiting the popularization of the bypass air-bleeding technology.

Disclosure of Invention

In view of one or more of the problems in the prior art, an aspect of the present invention provides a method for monitoring and disposing chlorine in a cement clinker production system for disposing fly ash generated by burning waste, the cement clinker production system comprising a cement kiln system, a bypass air discharging device (108), and an element detecting device, wherein the cement kiln system comprises a multi-stage preheater, a decomposing furnace (102), a smoke chamber (103), and a rotary kiln (104), raw materials for cement clinker production enter the smoke chamber (103) through the multi-stage preheater and the decomposing furnace (102), and the smoke chamber (103) is communicated with the rotary kiln (104); the bypass air discharging device (108) is communicated with the smoke chamber (103) and is used for discharging chlorine-containing smoke in the smoke chamber (103); the cement clinker production system further comprises a fly ash conveying device (114) for conveying the waste incineration fly ash into the cement kiln system; the method comprises the following steps:

s1) detecting the chloride ion content m in the hot raw meal delivered from the last preheater of the multi-stage preheaters to the smoke chamber (103) and the chloride ion content n in the cement clinker output from the rotary kiln (104) by using the element detection device, respectively, and calculating the chloride ion circulation ratio m/n in the cement kiln system;

s2) adjusting and controlling the technological parameters of the cement kiln system and/or the air release amount of the bypass air release device (108), and maintaining the chloride ion circulation multiplying power within the range of 50-500; preferably, the chloride ion cycle ratio is maintained within a range of 100 to 200.

In the above method, the adjusting and controlling the process parameters of the cement kiln system in step S2) specifically includes: A1) adjusting and controlling the temperature of the outlet of the decomposing furnace (102) to be 800-900 ℃; A2) and adjusting and controlling the temperature of a main burning zone in the rotary kiln (104) to be kept above 1400 ℃.

In the method, the method for adjusting and controlling the discharge amount of the bypass discharge device (108) in step S2) comprises the following steps: the adjustment is made in accordance with the chloride ion content in the hot raw meal and the trend of the chloride ion content in the hot raw meal, wherein the higher the chloride ion content in the hot raw meal, the greater the air release.

In the method, the element detection device comprises a hot raw meal detection device (107) and a clinker detection device (106), wherein the hot raw meal detection device (107) is used for detecting the content of chloride ions in the hot raw meal, and the clinker detection device (106) is used for detecting the content of chloride ions in the cement clinker; preferably, the hot raw meal detection device (107) and the clinker detection device (106) are XRF element detection devices.

In the method, the cement clinker production system further comprises solid waste and hazardous waste treatment equipment (115) which is respectively communicated with the fly ash conveying device (114) and the decomposing furnace (102), and the waste incineration fly ash enters the decomposing furnace (102) through the fly ash conveying device (114) and the solid waste and hazardous waste treatment equipment (115).

In the method, the cement clinker production system also comprises a bypass air-bleeding ash processing device (111) which is used for processing the bypass air-bleeding ash (110) separated from the bypass air-bleeding device (108); wherein the processing device (111) comprises:

the N water washing containers are named as a first water washing container, a second water washing container, … …, an N-1 th water washing container and an Nth water washing container respectively; n is more than or equal to 1; wherein each water washing container is used for generating solid-containing solution, and carrying out solid-liquid separation on the solid-containing solution to respectively obtain residual slurry residue and upper-layer solution; each water washing container is provided with a material inlet, a water solution outlet and a residual slurry and slag outlet, wherein for the first to the (N-1) th water washing containers, the residual slurry and slag outlet of the previous water washing container is communicated with the material inlet of the next water washing container; for the first water washing container to the Nth water washing container, the water solution outlet of the next water washing container is communicated with the material inlets of all the previous water washing containers;

the N stirring and heating devices are respectively arranged in the N washing containers and are used for uniformly mixing the solid-containing solution in the N washing containers;

a bypass air bleed ash reservoir (1) for receiving bypass air bleed ash separated from the bypass air bleed arrangement (108);

the bypass air-bleeding ash conveying device (2) is respectively communicated with the bypass air-bleeding ash storage (1) and the material inlets of the first water washing container (3) and is used for conveying the bypass air-bleeding ash in the bypass air-bleeding ash storage (1) to the first water washing container (3), and the first water washing container (3) is used for mixing the bypass air-bleeding ash in the bypass air-bleeding ash storage with an aqueous solution to form a first solid-containing solution;

the crystallizer (8) is provided with a brine inlet, a crystallized product outlet and a first condensed water outlet, wherein the brine inlet is communicated with the water solution outlet of the first washing container (3) and is used for receiving a first upper solution obtained by solid-liquid separation of a first solid-containing solution in the first washing container (3) and crystallizing the first upper solution;

a potassium chloride reservoir (9) which is communicated with a crystallization product outlet of the crystallizer (8) and is used for receiving a product separated out after the crystallization of the first upper layer solution by the crystallizer (8);

a condensate water container (10) which is provided with a condensate water inlet and a second condensate water outlet, wherein the condensate water inlet is communicated with the first condensate water outlet of the crystallizer (8), the second condensate water outlet is communicated with the material inlets of the N washing containers, and the condensate water in the condensate water container (10) is conveyed to one or more of the N washing containers to be used as an aqueous solution to form a solid-containing solution in the washing containers;

the clear water reservoir (21) is respectively communicated with the material inlets of the N water washing containers and is used for supplementing clear water to one or more of the N water washing containers;

and the residual slurry and residue storage (15) is communicated with the residual slurry and residue outlet of the Nth washing container and is used for receiving the Nth residual slurry and residue obtained after the solid-liquid separation of the Nth solid-containing solution in the Nth washing container.

The above method further comprises the steps of:

t1) conveying the bypass air-bleed ash separated from the bypass air-bleed device (108) to the first water washing container (3) to be mixed with an aqueous solution to form a first solid-containing solution; carrying out solid-liquid separation on the first solid-containing solution to respectively obtain first residual slurry residue and a first upper-layer solution;

t2) conveying the first residual slurry slag to a second washing container (12) to be mixed with an aqueous solution to form a second solid-containing solution, and carrying out solid-liquid separation on the second solid-containing solution to respectively obtain second residual slurry slag and a second upper layer solution; conveying the second residual slurry slag to a third washing container to be mixed with an aqueous solution to form a third solid-containing solution, and conveying the third residual slurry slag obtained after solid-liquid separation of the third solid-containing solution to a next-stage washing container; in the same way, until the N-1 th residual slurry residue obtained after the solid-liquid separation of the N-1 th solid-containing solution in the N-1 th washing container is conveyed to the N-1 th washing container to be mixed with the aqueous solution to form an N-1 th solid-containing solution, and the N-1 th residual slurry residue obtained after the solid-liquid separation of the N-1 th solid-containing solution in the N-1 th washing container is conveyed to the residual slurry residue storage (15); wherein N is more than or equal to 1;

wherein, for the first washing container (3) to the N-1 th washing container, the water solution for forming the solid-containing solution in the last washing container comes from the upper layer solution in the next washing container or containers, if the amount of the upper layer solution is insufficient, the water solution is supplemented by the condensed water from the condensed water container (10), and if the amount of the condensed water is insufficient, the water solution is supplemented by the clear water from the clear water container (21); wherein for a first cycle the aqueous solution in the first water wash vessel (3) for forming a first solids solution is taken from the clean water of the clean water reservoir (21); for the nth water wash vessel, wherein the aqueous solution used to form the nth solids solution is condensed water from the condensed water vessel (10), and if the amount of condensed water is insufficient, is replenished with fresh water from a fresh water reservoir (21);

t3) conveying the first upper solution to the crystallizer (8) for crystallization treatment to respectively obtain a crystallized product and condensed water;

t4) transferring the crystallized product to the potassium chloride reservoir (9) and transferring the condensed water to the condensed water container (10);

t5) conveying the condensed water of the condensed water container (10) to one or more water washing containers to be used as an aqueous solution to form a solid-containing solution in the water washing containers;

t6) repeating the above steps T1-T5.

In the method, the first upper solution is filtered before being conveyed to the crystallizer (8) in the step T3);

and the step T2) also comprises the step of conveying the Nth residual slurry residue in the residual slurry residue library (15) to a cement kiln system, preferably conveying the Nth residual slurry residue to a decomposing furnace (102) of the cement kiln system after being pretreated by the solid waste dangerous waste disposal equipment (115).

In another aspect, the present invention further provides a system for producing cement clinker by co-disposing fly ash from waste incineration, comprising:

a cement kiln system: the device comprises a multi-stage preheater, a decomposing furnace (102), a smoke chamber (103) and a rotary kiln (104), wherein raw materials for cement clinker production enter the smoke chamber (103) through the multi-stage preheater and the decomposing furnace (102), and the smoke chamber (103) is communicated with the rotary kiln (104);

bypass bleed (108): the smoke chamber is communicated with the smoke chamber (103) and is used for discharging chlorine-containing smoke in the smoke chamber (103);

a fly ash conveying device (114) for conveying the waste incineration fly ash into the cement kiln system;

element detection means for detecting the chloride ion content in the hot raw meal delivered by the last preheater of said multi-stage preheaters to said smokebox (103) and the chloride ion content in the cement clinker output from said rotary kiln (104);

a processing device (111) for processing the bypass air discharging ash separated from the bypass air discharging device (108).

The processing device (111) includes:

the N water washing containers are named as a first water washing container, a second water washing container, … …, an N-1 th water washing container and an Nth water washing container respectively; n is more than or equal to 1; wherein each water washing container is provided with a material inlet, a water solution outlet and a residual slurry and slag outlet, wherein for the first to the (N-1) th water washing containers, the residual slurry and slag outlet of the previous water washing container is communicated with the material inlet of the next water washing container; for the first water washing container to the Nth water washing container, the water solution outlet of the next water washing container is communicated with the material inlets of all the previous water washing containers;

The method for monitoring and disposing chlorine in the cement clinker production system for cooperatively disposing the waste incineration fly ash based on the technical scheme is a method for finely regulating and efficiently disposing the waste incineration fly ash and efficiently collecting chlorine elements, the method is characterized in that on the basis of the existing cement clinker production system, the chlorine ion content of hot raw materials and the chlorine ion content of cement clinker in a cement kiln system are respectively detected by an element detection device so as to monitor the chlorine elements in the system, and the chlorine ion circulation rate in the cement kiln system is accurately controlled to be maintained within the range of 50-500 by controlling the production process parameters of the cement kiln system and/or the air discharge quantity of a bypass air discharge device, so that the good and stable running state of the cement kiln system can be ensured, the chlorine ion content in the cement kiln system is dynamically balanced, and the influence of the chlorine elements in flue gas in the cement kiln system on the yield and quality of the cement clinker is avoided (the embodiment result shows that the chlorine ions can be stably obtained The cement clinker with low chlorine content with the average content of 0.018 percent meets the national standard and the internal standard of enterprises), and bypass air-bleed ash with high chlorine content (about 20 percent) can be obtained, and the potassium chloride product with high economic value can be obtained after the bypass air-bleed ash is washed by the treatment device provided by the invention. Compared with the prior art, the invention has the following beneficial effects:

1) the method provided by the invention can directly dispose and utilize the waste incineration fly ash by utilizing the existing cement clinker production system, so that the additional investment for constructing a huge fly ash washing pretreatment line is not needed, the cement clinker production line nearby a town can be fully utilized for nearby disposal, the additional investment for constructing a huge fly ash washing pretreatment line is not needed, a large amount of transportation cost is saved, and the disposal cost of the waste incineration fly ash is greatly reduced;

2) according to the method, the chloride ion circulation rate in the cement kiln system is controlled to be kept within the range of 50-500, so that the good and stable running state of the cement kiln system can be ensured, the chlorine element in the cement kiln system is dynamically balanced, and basically, the chlorine element does not enter a kiln skin of a burning zone in the form of alkali chloride, so that the thickness of the kiln skin is not increased and the rotation of a rotary kiln is not influenced, the influence of the chlorine element in flue gas in the cement kiln system on the yield and quality of cement clinker is avoided, the quality and yield of the cement clinker are obviously improved, in addition, the bypass air-release ash with high chlorine content (about 20%) can be continuously and stably obtained, the water washing treatment of the bypass air-release ash can be continuously and stably carried out, the high-economic-value potassium chloride product with the purity of more than 70% can be continuously obtained, and the utilization rate of waste is obviously improved;

3) when the method provided by the invention is used for producing cement clinker, a large amount of chlorine elements in the cement kiln system are discharged along with the bypass air-discharging ash, and the chlorine elements in the cement kiln system in each production cycle are small and controlled, so that a large amount of waste incineration fly ash can be treated each time, and the treatment efficiency of the waste incineration fly ash can be obviously improved;

4) when the treatment device in the cement clinker production system provided by the invention is used for treating the bypass discharged fly ash, the plurality of washing containers arranged in the treatment device are cooperated, so that the treatment efficiency of the bypass discharged air ash and the yield of a crystallized product (potassium chloride) can be obviously improved, the bypass discharged air ash generated under the condition that a cement clinker production line is cooperated to treat the normal capacity of the waste incineration fly ash can be completely dealt, and the accumulation of the bypass discharged air ash and the occupation of a large amount of space can not be caused. And the water resource can be repeatedly utilized in the processing device, and the final residual slurry slag is sent back to the cement kiln system or collected, stored and reused, so that the method is more environment-friendly.

Drawings

FIG. 1 is a schematic diagram of a system for producing cement clinker with co-disposal of fly ash from waste incineration according to an embodiment of the present invention;

FIG. 2 is a schematic structural diagram of a bypass blown ash handling device according to an embodiment of the present invention;

fig. 3 is a schematic flow chart of a bypass discharged ash processing device according to an embodiment of the present invention when processing bypass discharged ash.

1: bypass air-release ash warehouse, 2: bypass air-bleeding ash conveying device, 3: first water washing container, 4: first stirring and warming device, 5: brine filter equipment, 6: brine pumping valve, 7: brine pump, 8: crystallizer, 9: potassium chloride pool, 10: condensate container, 11: first residual slurry pump, 12: second water washing container, 13: second stirring and warming device, 14: second residual slurry pump, 15: residual slurry storage, 16: secondary water pumping valve, 17: secondary water pump, 18: condensate pump, 19: first clear water valve, 20: second clear water valve, 21: clearing the reservoir;

101: raw meal, 102: decomposing furnace, 103: smoke chamber, 104: rotary kiln, 105: clinker, 106: clinker detection device, 107: hot raw meal detection device, 108: bypass bleed, 109: residual gas, 110: bypass air bleeding ash, 111: processing apparatus, 112: treatment product, 113: waste incineration fly ash, 114: fly ash conveying device, 115: solid useless dangerous useless treatment facility.

Detailed Description

The invention aims to provide a method for cooperatively treating waste incineration fly ash by using a cement clinker production system and a system for jointly treating and utilizing waste incineration fly ash and bypass air discharge ash based on the cement clinker production system. The invention is illustrated in detail by the following specific examples and the accompanying drawings.

The embodiments are implemented on the premise of the technical scheme of the invention, and detailed implementation modes and specific operation processes are given, which are helpful for understanding the invention, but should not be taken as limiting the content of the invention.

Example 1: monitoring and disposal method for chlorine in cement clinker production system for cooperatively disposing waste incineration fly ash

As shown in fig. 1, the cement clinker production system on which the method provided by this embodiment is based may include: the cement kiln system, the element detection device, the bypass air discharging device 108 and the fly ash conveying device 114 can also comprise solid waste and hazardous waste disposal equipment 115.

The cement kiln system may be an existing dry cement clinker production system comprising a multi-stage preheater (in this example, five-stage preheaters C1-C5), a decomposing furnace 102, a smoke chamber 103, a rotary kiln 104, etc., and raw materials (i.e., raw materials 101) for cement clinker production first enter a C1 preheater, then sequentially pass through a C3 preheater, a C2 preheater, a C4 preheater, then enter the decomposing furnace 102, then enter a C5 preheater, and then enter the smoke chamber 103 through a discharge tube at a material outlet of the C5 preheater, at which time these materials are referred to as hot raw materials. The hot raw meal is then fed from the flue chamber 103 into the rotary kiln 104, and the material is calcined after being fed into the rotary kiln 104 to produce a cement clinker product (i.e., clinker 105).

The element detection device is used for detecting the content of chloride ions in the hot raw materials and the cement clinker, and can select the existing element detection device based on the chemical or X-ray fluorescence spectrum analysis principle in the prior art, for example, the XRF element detection device based on the X-ray fluorescence spectrum analysis principle, and can detect the content of the chloride ions in the hot raw materials and the clinker off line periodically (for example, at intervals of 1-2 hours). It is also possible to use the hot raw meal detection means 107 for detecting the content of chloride ions in the hot raw meal and the clinker detection means 106 for detecting the content of chloride ions in the clinker as shown in fig. 1, wherein both may be provided as on-line detection element detection means, or only the hot raw meal detection means 107 may be provided as on-line detection means, in order to avoid the influence of on-site production equipment and environment on operators.

The bypass air discharging device 108 can adopt the existing equipment, and is communicated with the smoke chamber 103, so as to discharge chlorine-containing flue gas brought into the cement kiln system from the smoke chamber 103 from cement production raw materials, coal and waste incineration fly ash, co-disposed solid waste hazardous waste and the like, and avoid the influence of chlorine on the quality and yield of cement clinker products produced in the cement kiln production system. The part of chlorine-containing flue gas exhausted from the cement kiln system is separated into bypass air-bleeding ash 110 containing potassium chloride by a bypass air-bleeding device 108, and residual gas 109 carrying heat gas and a small amount of solids enters an exhaust system for further utilization (such as waste heat power generation and the like). The separated by-pass bleed ash 110 contains a large amount of chlorine and can be subjected to subsequent treatment (e.g., water washing) to obtain a potassium chloride product of high economic value, as described in detail in examples 2 and 3 below.

The solid waste hazardous waste disposal equipment 115 may be existing equipment commonly used in cement clinker production lines, such as cement kiln SMP (crushing, mixing, pumping) pretreatment equipment, cement kiln sludge disposal equipment, etc., and may be treated in advance before the waste incineration fly ash is put into a decomposing furnace of a cement kiln system.

The fly ash adding device 114 is used for adding the waste incineration fly ash 113 into the decomposing furnace 102 of the cement kiln system, and the fly ash adding device 114 can also be communicated with the solid waste dangerous waste disposal equipment 115 firstly, so that the waste incineration fly ash 113 is conveyed into the solid waste dangerous waste disposal equipment 115 to be pretreated with other solid waste dangerous waste disposals, and then is put into the decomposing furnace 102 of the cement kiln system.

Referring to fig. 1, in a typical dry cement kiln system, raw production materials (raw meal 101) enter a C1 preheater, then pass through a C3 preheater, a C2 preheater, a C4 preheater in that order, then enter a calciner 102, then enter a C5 preheater, and then enter a kiln tail gas chamber 103 through the C5 preheater material outlet, where they are referred to as hot raw meal. The hot raw materials enter the rotary kiln 104 from the kiln tail smoke chamber 103, and the materials are calcined (the calcination temperature is generally 1300-1500 ℃) after entering the rotary kiln 104 to generate cement clinker. The clinker produced is cooled by fresh cold air after leaving the kiln head, and the air used for cooling the clinker is rapidly heated, which is called hot gas. If the flow of raw material in the cement kiln system is a forward direction, the flow of hot gas is substantially a reverse direction. The high-temperature gas passes through the rotary kiln 104 (one part of the high-temperature gas directly enters the decomposing furnace 102), the kiln tail smoke chamber 103, the decomposing furnace 102 and the multi-stage preheater, the temperature of the high-temperature gas is reduced to 300-350 ℃ after the high-temperature gas is discharged out of the C1 preheater, and then the high-temperature gas is discharged out of the cement kiln system. The purpose of this is to make full use of the heat energy, and to make full heat exchange between the material and the gas in each stage, so that the material is gradually heated before entering the rotary kiln 104, and the high temperature gas is gradually cooled.

When the cement kiln system works, chlorine element enters the rotary kiln 104 and the decomposing furnace 102 in the form of a plurality of compounds through fire coal, or enters a C1 preheater in the form of chloride salt in raw materials (raw materials 101), or enters the decomposing furnace 102 in the form of sodium chloride, ferric chloride and the like through co-disposal solid waste hazardous waste. Chlorine element in the co-disposed waste incineration fly ash can also enter the decomposing furnace 102. These chlorine elements in various forms are finally combined with potassium elements in the raw materials to form potassium chloride under the action of high temperature in the cement kiln system. For example: sodium chloride in the raw materials and the inorganic hazardous wastes can react with potassium oxide in the clinker at high temperature in the kiln to directly generate potassium chloride; or the PVC plastics in the solid waste generate hydrogen chloride when being combusted at high temperature in the cement kiln system, the hydrogen chloride is quickly absorbed by calcium oxide in the materials to generate calcium chloride, and the calcium chloride is further exchanged with potassium oxide in the materials at high temperature in the rotary kiln to generate potassium chloride gas. The boiling point of potassium chloride is 1420 ℃ and the melting point is 770 ℃. And the sublimation volatilization starts at 800 ℃, and the volatilization is faster at higher temperature.

Thus, as the material is progressively warmed in each process step, the potassium chloride also progressively changes to a gaseous state, and eventually substantially all changes to a gaseous state at the higher temperatures within the rotary kiln 104, as viewed in conjunction with the direction of flow of the material within the cement kiln system. The gaseous potassium chloride flows in the opposite direction with the high temperature gas. As the gas temperature decreases, the gaseous potassium chloride begins to condense, forming solid microcrystalline particles, which are adhered to by the material and are once again positively carried back into the rotary kiln 104. In general, the concentration of gaseous potassium chloride in the kiln tail gas chamber 103 is relatively high. And the content of chlorine element in the solid material in the charging barrel at the material outlet of the C5 preheater is higher.

Although the higher temperatures within the rotary kiln 104 allow the potassium chloride to be substantially entirely gaseous, it is inevitable that a portion of the chlorine remains in the clinker and is carried out of the kiln system with the clinker. However, compared with the fire coal and raw materials with higher chlorine content, especially all the chlorine elements brought by the co-processing of the chlorine-containing solid waste hazardous wastes, the chlorine elements carried away by the clinker have smaller proportion. Obviously, potassium chloride will be concentrated and recycled within the cement kiln system, and if left to develop, its concentration will be increasingly high and uncontrolled, thereby affecting the yield and quality of cement clinker. Therefore, a bypass air discharging device communicated with the smoke chamber is needed to discharge a part of chlorine-containing flue gas and discharge redundant potassium chloride out of the cement kiln system, but the prior art methods cannot give consideration to both avoiding the influence of the chlorine-containing flue gas in the cement kiln system on the yield and quality of cement clinker, obtaining treated bypass air discharging ash with high economic value, and maintaining the dynamic balance of the chlorine element content in the cement kiln system to ensure that the running state of the cement kiln system is good and stable.

In this embodiment, a typical cement clinker production system is used to cooperatively dispose waste incineration fly ash, wherein an element detection device is used to monitor the content of chloride ions in hot raw materials and the content of chloride ions in cement clinker in the system to control the content of chloride ions in the system, so as to avoid the influence of chlorine-containing flue gas in a cement kiln system on the yield and quality of cement clinker, obtain bypass air-release ash with high chloride content (high utilization value), and maintain the dynamic balance of the content of chloride elements in the cement kiln system to ensure the good and stable operation state of the cement kiln system, as shown in fig. 1, the method specifically includes the following steps:

s1: feeding the waste incineration fly ash 113 into the cement kiln decomposing furnace 102 by using a fly ash conveying device 114; or, the waste incineration fly ash 113 is sent into the solid waste hazardous waste disposal equipment 115 for pretreatment by the fly ash conveying device 114 according to the solid waste hazardous waste disposal substances, and then sent into the cement kiln decomposing furnace 102 by the solid waste hazardous waste disposal equipment 115;

s2: the raw materials for cement clinker production (i.e. raw meal 101) are fed into the cement kiln system via a C1 preheater;

s3: respectively detecting the content m of chloride ions in hot raw meal conveyed from the last stage preheater of the multi-stage preheater to a smoke chamber (103) and the content n of chloride ions in cement clinker output from a rotary kiln (104) by using an element detection device, and calculating the chloride ion circulation ratio in a cement kiln system to be m/n; wherein the content m of chloride ions in the hot raw meal can be detected by using a hot raw meal detection device 107, and the content n of chloride ions in the clinker can be detected by using a clinker detection device 106;

s4: and adjusting and controlling the technological parameters of the cement kiln system and/or the air discharge amount of the bypass air discharge device (108), and maintaining the chloride ion circulation rate within the range of 50-500, preferably within the range of 100-200 (the obtained cement clinker in different batches has smaller fluctuation of the chloride ion content, relatively lower content and more stable running state of the cement kiln system).

For example, when adjusting and controlling the process parameters of the cement kiln system, the following parameters can be specifically adopted: A1) and adjusting and controlling the temperature of the outlet of the decomposing furnace (102) to be 800-900 ℃, and further controlling the temperature of the hot raw meal in the discharging barrel at the material outlet of the C5 preheater. The liquid phase of the materials can not be generated in advance or in a small proportion before the materials enter the main burning zone, and the situation that the potassium chloride is wrapped in the clinker by early balling is avoided; A2) the temperature of the main burning zone in the rotary kiln (104) is regulated and controlled to be kept above 1400 ℃, preferably 1400-1500 ℃, so that clinker is slow in granulation, uniform in granules, and potassium chloride is fully volatilized and gasified. The air discharge amount of the bypass air discharge device can be adjusted according to the total amount of potassium chloride in the system calculated by the absolute value of the content of chloride ions in the hot raw meal (the higher the content of chloride ions in the hot raw meal is, the larger the bypass air discharge amount is), and the chlorine ion content in the hot raw meal tends to be stable according to the variation trend of the content of chloride ions in the hot raw meal, so that the chlorine element newly added into the cement kiln system and the discharged chlorine element can be kept in dynamic balance.

The chlorine content in the cement kiln system can be maintained in dynamic balance through the accurate control of the chloride ion circulation multiplying power in the cement kiln system in the steps, the cement kiln system is ensured to run well and stably, the content of chloride ions brought into cement clinker is remarkably lower compared with that of other chloride ion circulation multiplying powers, and the kiln skin of the rotary kiln cannot be thickened, so that the yield and the quality of cement clinker products can be ensured to be stable, and meanwhile, flue gas with high chlorine content can be stably and continuously discharged from the cement kiln system;

s5: the bypass air-bleed device 108 separates the bypass air-bleed ash 110 containing potassium chloride from the chlorine-containing flue gas, wherein the content of chloride ions can reach about 20%, so that the economic benefit of further treatment of the flue gas can be improved (for example, the water washing treatment can obtain a potassium chloride product with high economic value).

In summary, the method provided by this embodiment can not only avoid the influence of the chlorine-containing flue gas in the cement kiln system on the yield and quality of cement clinker, but also discharge the chlorine-containing flue gas with high economic value from the cement kiln system, and maintain the dynamic balance of the chlorine content in the cement kiln system to ensure the good and stable operation state of the cement kiln system, and has the following advantages: before the waste incineration fly ash enters the system, the fly ash does not need to be subjected to washing pretreatment, cement clinker production lines near cities and towns can be fully utilized for nearby disposal, and additional investment for constructing a huge fly ash washing pretreatment line is not needed, so that a large amount of transportation cost and washing pretreatment cost can be saved, the disposal cost of the waste incineration fly ash can be greatly reduced, the waste incineration fly ash is effectively utilized, cement clinker products with high yield and quality are obtained, and a foundation is laid for further treating high-chlorine-content bypass discharged air ash to obtain high-economic-value potassium chloride products.

Example 2: cement clinker production system for cooperatively disposing waste incineration fly ash

As shown in fig. 1, a schematic structural diagram of a cement clinker production system for co-disposing waste incineration fly ash provided by this embodiment is shown, and the system further includes a bypass air-bleed ash treatment device 111 on the basis of embodiment 1, so as to perform water washing treatment on the bypass air-bleed ash 110 with high chlorine content separated by the bypass air-bleed device 108, so as to obtain a treatment product 112 with high economic value, such as potassium chloride. The rest residues after the water washing treatment can be sent into solid waste and hazardous waste treatment equipment 115 according to solid waste and hazardous waste treatment substances to be premixed with the waste incineration fly ash, and then enter a decomposing furnace 102 of the cement kiln system, or the part of residues is collected for other use. Can further improve the treatment depth of the waste incineration fly ash and the utilization rate of waste.

As shown in fig. 2, the processing device 111 mainly includes: the system comprises a first washing container 3, a second washing container 12, a crystallizer 8, a condensed water container 10, a bypass air-bleeding ash storehouse 1, a potassium chloride storehouse 9, a residual slurry-slag storehouse 15, a clear water storehouse 21, a bypass air-bleeding ash conveying device 2, a brine filtering device 5 arranged between the first washing container 3 and the crystallizer 8, pipelines used for connecting all parts, and pumps, valves and the like arranged among all parts.

The bypass air discharging ash storeroom 1 is used for receiving bypass air discharging ash 110 separated from the bypass air discharging device 108; the bypass air-discharging ash conveying device 2 is respectively communicated with the bypass air-discharging ash warehouse 1 and the first washing container 3 and is used for conveying bypass air-discharging ash in the bypass air-discharging ash warehouse 1 to the first washing container 3, the first washing container 3 is used for mixing the bypass air-discharging ash in the bypass air-discharging ash warehouse and an aqueous solution (such as clear water from a clear water reservoir 21) into a first solid-containing solution, and the first stirring and heating device 4 is used for stirring and mixing the first solid-containing solution and heating if necessary so as to uniformly mix the first solid-containing solution and fully dissolve potassium chloride in the bypass air-discharging ash; the crystallizer 8 is communicated with the first washing container 3 and is used for receiving a first upper solution obtained by solid-liquid separation of a first solid-containing solution in the first washing container 3 and carrying out potassium chloride crystallization on the first upper solution, wherein a brine filtering device 5 is arranged between the first washing container 3 and the crystallizer 8 so as to filter the first upper solution, the filtered first upper solution is conveyed into the crystallizer 8 through a brine pump 7, and a brine pumping valve 6 is arranged on a pipeline between the first washing container 3 and the crystallizer 8; the potassium chloride storage 9 is communicated with the crystallizer 8 and is used for receiving potassium chloride separated out after the first upper layer solution is crystallized by the crystallizer 8; a condensate water container 10 is communicated with the crystallizer 8 and is used for receiving condensate water generated by crystallizing the first upper layer solution through the crystallizer 8; the condensate water container 10 is also in communication with the first washing container 3 and the second washing container 12, respectively, via a pipe for conveying condensate water in the condensate water container 10 to the first washing container 3 and/or the second washing container 12, for example via a condensate water pump 18; the second washing container 12 is configured to receive first residual slurry obtained by solid-liquid separation of the first solid-containing solution in the first washing container 3 (for example, the first residual slurry in the first washing container 3 is pumped into the second washing container 12 by the first residual slurry pump 11), and mix the first residual slurry with the aqueous solution to form a second solid-containing solution, and the second stirring and heating device 13 is configured to stir and mix the second solid-containing solution, and perform a heating operation if necessary, so as to uniformly mix the second solid-containing solution and fully dissolve residual potassium chloride in the first residual slurry; the clear water reservoir 21 is respectively communicated with the first washing container 3 and the second washing container 12, a first clear water valve 19 is arranged between the clear water reservoir and the first washing container 3, and a second clear water valve 20 is arranged between the clear water reservoir and the second washing container 12 and is used for supplementing clear water to the first washing container 3 and the second washing container 12; the residual slurry storage 15 is configured to receive the second residual slurry obtained by performing solid-liquid separation on the second solid-containing solution in the second water washing container 12 (for example, the second residual slurry in the second water washing container 12 is pumped into the residual slurry storage 15 by the second residual slurry pump 14), and the residual slurry in the residual slurry storage 15 may also be conveyed to the solid waste hazardous waste disposal device 115. The second upper solution (i.e. the second solution) obtained by solid-liquid separation of the second solid-containing solution in the second washing container 12 is conveyed into the first washing container 3 through a pipeline (for example, through a secondary water pump 17) to be uniformly mixed with the bypass air-released ash to form the first solid-containing solution.

The processing device 111 shown in fig. 2 includes only two water washing containers, and it should be understood by those skilled in the art that, in order to increase the washing rate of potassium chloride in the bypass air-released ash, the processing device 111 for washing the bypass air-released ash water provided in this embodiment may further include more water washing containers (for example, N water washing containers, N ≧ 1), and a stirring and heating device matched with the water washing containers and components such as pipes, valves, and water pumps, so as to form a circulation system for performing a water washing operation on the bypass air-released ash. The N water washing containers are named as a first water washing container, a second water washing container, … …, an N-1 water washing container and an Nth water washing container respectively; n is more than or equal to 1; wherein each water washing container is provided with a material inlet, a water solution outlet and a residual slurry and slag outlet, wherein for the first to the (N-1) th water washing containers, the residual slurry and slag outlet of the previous water washing container is communicated with the material inlet of the next water washing container; for the first water washing container to the Nth water washing container, the water solution outlet of the next water washing container is communicated with the material inlets of all the previous water washing containers. The connection relation and the working principle of the treatment device are illustrated by taking N as 4, the four water washing containers are named as a first water washing container, a second water washing container, a third water washing container and a fourth water washing container respectively, wherein the first residual slurry residue obtained after the solid-liquid separation of the first solid-containing solution in the first washing container enters a second washing container to be mixed with the aqueous solution to form a second solid-containing solution, the second residual slurry and slag after the solid-liquid separation of the second solid-containing solution enter a third washing container to be mixed with the aqueous solution to form a third solid-containing solution, the third residual slurry and slag after solid-liquid separation of the third solid-containing solution enter a fourth washing container to be mixed with the aqueous solution to form a fourth solid-containing solution, and discharging the fourth residual slurry after solid-liquid separation of the fourth solid-containing solution out of the circulating system and entering a residual slurry warehouse (the residual slurry in the residual slurry warehouse can be sent into solid waste hazardous waste disposal equipment and then enter a cement kiln system again or be collected for other use). Wherein in the first circulation, the water solution for forming the first solid-containing solution in the first water washing container comes from clear water of the clear water reservoir, and in the subsequent circulation, the upper layer solution of the solid-liquid separation of the solid-containing solution in one or more of the second water washing container, the third water washing container and the fourth water washing container is preferably the second upper layer solution of the solid-liquid separation of the second solid-containing solution in the second water washing container in sequence, replenishing a third upper layer solution after solid-liquid separation of a third solid-containing solution in a third water washing container, if the amount of the third upper layer solution is insufficient, then the fourth upper solution after solid-liquid separation of the fourth solid-containing solution in the fourth washing container is supplemented, and if the amount of the fourth upper solution is supplemented, the amount is still insufficient, the condensed water from the condensed water container is replenished, and if the amount of the condensed water is insufficient, the clear water from the clear water reservoir is replenished. The aqueous solution for forming the second solid-containing solution in the second washing container is an upper solution obtained by solid-liquid separation of the solid-containing solution in one or more of the third washing container and the fourth washing container, preferably a third upper solution obtained by solid-liquid separation of the third solid-containing solution in the third washing container, if the amount of the third upper solution is insufficient, the fourth upper solution obtained by solid-liquid separation of the fourth solid-containing solution in the fourth washing container is supplemented, if the amount of the fourth upper solution is insufficient, the condensed water from the condensed water container is supplemented, and if the amount of the condensed water is insufficient, the clear water from the clear water reservoir is supplemented. Likewise, the same is true of the source of the aqueous solution in the third wash vessel. The fourth water washing container is used for forming the aqueous solution containing the solid solution, the condensed water in the condensed water container is obtained, and if the amount of the condensed water is insufficient, the clear water from the clear water reservoir is supplemented.

And the first upper layer solution of the first solid-containing solution in the first washing container after solid-liquid separation enters a crystallizer for crystallization, and the generated condensed water returns to one or more of the four washing containers to form the solid-containing solution. Therefore, the processing device for washing the bypass discharged air ash can recycle water resources, and can effectively extract potassium chloride products with high economic value in the bypass discharged air ash.

Example 3: method for treating bypass discharged air ash by utilizing treatment device

In this embodiment, the processing device 111 in the cement clinker production system provided in embodiment 2 is used to perform water washing processing on the bypass air-bleeding ash separated by the bypass air-bleeding device 108, and as shown in fig. 2 and 3, the method mainly includes the following steps:

t1: opening the bypass air-bleeding ash conveying device 2, and conveying a proper amount of bypass air-bleeding ash to the first washing container 3;

t2: opening a secondary water pumping valve 16, opening a secondary water pump 17, and sending the second upper solution (i.e. the second solution in fig. 2 and 3) subjected to solid-liquid separation in the second water washing container 12 to the first water washing container 3 through the secondary water pump 17; replenishing the condensate from the condensate container 10 if the second solution is insufficient, and replenishing the clear water from the clear water reservoir 21 to the first wash container 3 if the condensate is insufficient or at the first duty cycle by opening the first clear water valve 19;

t3: after the pumping of the upper layer second solution subjected to solid-liquid separation in the second washing container 12 is completed, the second residual slurry pump 14 is opened, and the second residual slurry left in the second washing container 12 is pumped to the residual slurry storage 15; the first duty cycle may skip this step;

t4: while the step T3 is being performed, the first stirring and heating device 4 is operated to stir (heat if necessary) the first solid-containing solution in the first washing container 3 to sufficiently dissolve the potassium chloride in the bypass air-bleeding ash in the second solution;

t5: after the first solid-containing solution in the first washing container 3 is stood, solid-liquid separation is carried out, the upper layer is nearly saturated potassium chloride brine (namely the first solution in figure 3), and the lower layer is first residual slurry residue. Opening a brine pumping valve 6, opening a brine pump 7, and pumping the potassium chloride brine on the upper layer to a crystallizer 8 (wherein the brine is filtered by a brine filtering device 5);

t6: after the potassium chloride brine on the upper layer in the first washing container 3 is pumped, the first residual slurry pump 11 is started, and the first residual slurry on the lower layer in the first washing container 3 is pumped into the second washing container 12;

t7: while the step T6 is performed, the crystallizer 8 works to separate out potassium chloride crystals in the potassium chloride brine and send the potassium chloride crystals into a potassium chloride storage 9; condensed water generated by crystallization is sent into a condensed water container 10;

t8: after the first residual sludge in the step T6 is pumped into the second washing container 11, the condensed water pump 18 is turned on, and the condensed water in the condensed water container 10 is pumped into the second washing container 12; if the condensed water is insufficient, opening a second clear water valve 20, and replenishing clear water from a clear water reservoir 21 to a second washing container 12;

t9: the second stirring and heating device 13 works to stir the second solid-containing solution in the second washing container 12, and fully dissolve the residual potassium chloride in the first residual slurry residue in the condensed water (or clear water);

t10: and after the second solid-containing solution in the second washing container 12 is kept stand, performing solid-liquid separation, wherein the upper layer is the second solution with low potassium chloride content, and the lower layer is the second residual slurry residue. Waiting for the next cycle of use;

wherein the pump, the valve and the stirring and heating device which are opened in each step are closed after the step is finished.

And repeating the steps T1 to T10, wherein the steps are staggered and separated by one period of time. Therefore, the bypass air-bleed ash can be continuously washed by water to continuously obtain a crystalline product, such as a potassium chloride product, and the purity of the obtained potassium chloride product can reach more than 70%.

Example 4: application examples

This example illustrates the practical effect of the method and system of the present invention in a cement clinker production line producing 5000 tons per day.

First, the following scale water wash bypass air release ash line was established. 2 tons of the bypass air discharge ash of each circulation water washing are calculated by the content of chloride ions in the bypass air discharge ash of 20%, each circulation participated water is about 6 tons, and the volume of the water washing container can be 8-15 cubic meters, preferably about 10 cubic meters. Overlapping the time required by the steps of ash feeding, water adding, stirring and heating, standing and separating and the like, and calculating each water washing period to be about 80-150 minutes, preferably 90-120 minutes. Thus, if the continuous operation is carried out, at least 20 tons of bypass air-discharging ash can be washed by water every day, and the requirement of a cement clinker production line is met. And provides room for increasing the ash discharge amount of bypass air discharge ash when the cement kiln system directly disposes the waste incineration fly ash. The capital investment of the production line equipment of the water-washing bypass air-bleeding ash line with the scale is not more than 500 ten thousand.

The content of chlorine element in the fly ash is about 6-12%, and the production line of the water-washing bypass air-discharging ash line can treat at least 30-40 tons of waste incineration fly ash per day according to the average 10%. Compared with the prior mode of intensively carrying out water washing pretreatment on the waste incineration fly ash, the method has low equipment investment. Compared with the prior method for disposing the fly ash after the water washing pretreatment, the method for directly disposing the waste incineration fly ash and washing the bypass discharged air ash by the cement kiln has the advantages that the equipment cost is about one fourth or even lower, and the transportation cost is greatly reduced. Compared with the prior art, the method provided by the invention can not only avoid the influence of chlorine-containing flue gas in the cement kiln system on the yield and quality of cement clinker, but also efficiently utilize the chlorine-containing flue gas discharged from the cement kiln system to obtain a potassium chloride product with high economic value through more accurate control (the circulation rate of chloride ions in the cement kiln system is kept within the range of 50-500), and can maintain the dynamic balance of the content of chlorine elements in the cement kiln system to ensure that the running state of the cement kiln system is good and stable.

Taking the implementation of a cement clinker production enterprise in Jiangsu as an example, the method and the cement clinker production system (the system) provided by the invention have the following effects:

before the system is implemented, the enterprise is also provided with a bypass air discharging device, but the content of chlorine ions in the discharged bypass air discharging ash is generally not more than 10%, and the discharged bypass air discharging ash is piled up and treated, so that the occupied area is large. In addition, the enterprise also has an SMP system for the cooperative disposal of solid waste and hazardous waste. However, the content of chlorine in the treated solid waste and hazardous waste is high, the chlorine elements cannot be efficiently discharged through the bypass air discharging device, the content of chloride ions in the cement clinker exceeds the index of 0.027% controlled by an enterprise in most batches when the SMP system runs, and in order to obtain the cement clinker meeting the quality requirement, the operation of the SMP system needs to be stopped at the moment. Therefore, the SMP system cannot be put into production all the time by coordinating and handling, and the enterprise benefit is influenced.

After the system is implemented, the kiln conditions are adjusted, the total amount of potassium chloride discharged from the system is kept equivalent to the equivalent amount of chlorine element newly added in the system, and the circulation rate of chloride ions is kept within the range of 50-500, so that the chlorine element in the cement kiln system is in a stable equilibrium state. The clinker production is not only free from the problems of crust formation, rolling large balls, over standard clinker chlorine content and the like caused by high chloride ion content in the prior art, but also improves the productivity due to stable kiln conditions. More importantly, the SMP system which is used for cooperatively treating solid waste and hazardous waste is put into production.

Specifically, in the cement kiln system after the production line is adjusted, the content of chloride ions in clinker is averagely 0.018%, the clinker is relatively stable, meets national standards and enterprise internal standards, and is averagely reduced by more than 0.01% compared with the SMP system before adjustment; the content of chloride ions in the hot raw material is between 1.8 and 3.0 percent; the circulation ratio is controlled to be about 100-160. The chlorine ion content of the bypass air discharge ash is kept between 16 and 22 percent, and the content of the converted potassium chloride is about 30.3 to 41.7 percent. Under the condition that the enterprise bypass air discharging device discharges 0.5 ton of ash per hour, the pulp slag sent into the decomposing furnace by the SMP system can be treated by 10 tons of pulp slag per hour when the chloride ion content is 0.8% on average.

The enterprise also carries out water washing treatment on the bypass air-bleeding ash with high chlorine content, establishes a two-stage water washing production line (namely, comprises two water washing containers), and can wash 1 ton of bypass air-bleeding ash in each circulation. The proportion of the ash water is prepared according to the average 20 percent of the chloride ion content in the bypass air-bleed ash, each circulation participates in about 3 tons of water, and the volume of the water washing container is 5 cubic meters. Each washing cycle is about 2 hours, at least 10 tons of bypass air-discharging ash can be treated every day, the operation requirement of enterprises on cooperative treatment of solid waste and hazardous waste SMP is met, and the economic benefit is obvious. And the potassium chloride salt with the purity of more than 70 percent is produced about 5 tons every day, and the bypass air-release ash is not required to be accumulated, so that the site burden is solved for enterprises, and the income is increased.

Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A monitoring and disposal method for chlorine in a cement clinker production system for cooperatively disposing waste incineration fly ash, wherein the cement clinker production system comprises a cement kiln system, a bypass air discharging device (108) and an element detection device, the cement kiln system comprises a multi-stage preheater, a decomposing furnace (102), a smoke chamber (103) and a rotary kiln (104), raw materials for cement clinker production enter the smoke chamber (103) through the multi-stage preheater and the decomposing furnace (102), and the smoke chamber (103) is communicated with the rotary kiln (104); the bypass air discharging device (108) is communicated with the smoke chamber (103) and is used for discharging chlorine-containing smoke in the smoke chamber (103); characterized in that the cement clinker production system further comprises a fly ash conveying device (114) for conveying the waste incineration fly ash into the cement kiln system; the method comprises the following steps:

2. The method as claimed in claim 1, wherein the adjusting and controlling the process parameters of the cement kiln system in step S2) is specifically: A1) adjusting and controlling the temperature of the outlet of the decomposing furnace (102) to be 800-900 ℃; A2) and adjusting and controlling the temperature of a main burning zone in the rotary kiln (104) to be kept above 1400 ℃.

3. The method according to claim 1 or 2, characterized in that the method for adjusting and controlling the bleed air amount of the bypass bleed device (108) in step S2) is: the adjustment is made in accordance with the chloride ion content in the hot raw meal and the trend of the chloride ion content in the hot raw meal, wherein the higher the chloride ion content in the hot raw meal, the greater the air release.

4. A method according to any one of claims 1-3, characterized in that the element detection means comprise a hot raw meal detection means (107) and a clinker detection means (106), wherein the hot raw meal detection means (107) are adapted to detect the content of chloride ions in the hot raw meal and the clinker detection means (106) are adapted to detect the content of chloride ions in the cement clinker;

preferably, the hot raw meal detection device (107) and the clinker detection device (106) are XRF element detection devices.

5. The method according to any one of claims 1 to 4, wherein the cement clinker production system further comprises a solid waste hazardous waste disposal facility (115) which is in communication with the fly ash conveying device (114) and the decomposing furnace (102), respectively, and the waste incineration fly ash is passed through the fly ash conveying device (114) and the solid waste hazardous waste disposal facility (115) and then enters the decomposing furnace (102).

6. A method according to any of claims 1-5, characterized in that the cement clinker production system further comprises a treatment device (111) of bypass air bleed ash for treating bypass air bleed ash (110) separated from the bypass air bleed device (108); wherein the processing device (111) comprises:

7. The method of claim 6, further comprising the steps of:

t6) repeating the above steps T1-T5.

8. The method according to claim 7, characterized in that the first upper solution is also filtered before being sent to the crystallizer (8) in step T3);

9. A cement clinker production system for co-processing waste incineration fly ash is characterized by comprising:

10. The system according to claim 9, characterized in that said processing means (111) comprise: