WO2020182012A1 - 多级悬浮预热水泥窑炉系统及其控制方法 - Google Patents

多级悬浮预热水泥窑炉系统及其控制方法 Download PDF

Info

Publication number
WO2020182012A1
WO2020182012A1 PCT/CN2020/077539 CN2020077539W WO2020182012A1 WO 2020182012 A1 WO2020182012 A1 WO 2020182012A1 CN 2020077539 W CN2020077539 W CN 2020077539W WO 2020182012 A1 WO2020182012 A1 WO 2020182012A1
Authority
WO
WIPO (PCT)
Prior art keywords
coal
heat exchange
cyclone
preheater
stage
Prior art date
Application number
PCT/CN2020/077539
Other languages
English (en)
French (fr)
Inventor
任强强
蔡军
吕清刚
Original Assignee
中国科学院工程热物理研究所
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 中国科学院工程热物理研究所 filed Critical 中国科学院工程热物理研究所
Publication of WO2020182012A1 publication Critical patent/WO2020182012A1/zh

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C04B7/434—Preheating with addition of fuel, e.g. calcining
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D13/00—Apparatus for preheating charges; Arrangements for preheating charges

Definitions

  • the embodiments of the present invention relate to the field of nitrogen oxide emission control in the cement industry, and in particular to a multi-stage suspension preheating cement kiln system and a control method thereof.
  • the cement production process commonly used at home and abroad is the new dry cement production process, in which the rotary kiln and the calciner are the main equipment in the process.
  • Rotary kiln is the final firing device for cement clinker. Due to the gas-solid accumulation heat transfer in the kiln, the heat transfer effect is poor. In order to obtain high-quality cement clinker, the kiln head calcining gas temperature is as high as 1800°C, which causes the thermal power of the rotary kiln. Type NO x emissions are extremely high, accounting for more than 80% of all thermal NO x emissions. Moreover, in view of the characteristics of the high-temperature calcination process of the rotary kiln, the generation of this part of the thermal NO x cannot be avoided.
  • the calciner is a cement raw meal decomposition device.
  • the decomposition of cement raw meal in the calciner needs to absorb a large amount of heat, which is provided by the combustion of pulverized coal. Therefore, the amount of coal required for combustion in the calciner is higher than that required for combustion in the rotary kiln. the amount of coal (about 60% to account for all of the coal), so that the fuel type NO x emissions precalcinor higher.
  • Rotary kilns and calciners are currently the two main sources of NO x emissions from the new dry-process cement production process, causing the overall NO x emissions of cement kilns to be at a relatively high level, with the original emissions exceeding 1000 mg/Nm 3 .
  • Statistics show that the cement industry’s NO x emissions in 2017 accounted for 10-12% of the country’s total NO x emissions, which is one of the important causes of haze weather in China, which seriously endangers the atmospheric environment and human health. It can be seen that achieving low NO x emissions from cement kilns has important strategic significance for air pollution control.
  • China's cement industry NO x emission standard stipulates that the NO x emission control level in key areas is not higher than 320mg/Nm 3 , and in general areas it is not higher than 400mg/Nm 3 , and some local provinces, cities and regions have even proposed higher levels.
  • Emission Standards For example, Jiangsu province stipulates that the cement industry's NO x emission cannot be higher than 100mg/Nm 3 before June 1, 2019; Henan province stipulates that before October 2018, the NO x concentration of cement companies after transformation is not high under the condition of a baseline oxygen content of 10% At 150mg/Nm 3 .
  • staged combustion technology In addition to SNCR technology, calciner fuel/air staged combustion technology has always been valued by cement companies.
  • the staged combustion technology is to distribute the pulverized coal fuel used in the decomposition furnace or the air used for fuel combustion at multiple points to create as many reducing atmosphere areas as possible while ensuring the fuel combustion efficiency. On the one hand, it reduces the generation of NO x . On the other hand, the NO x from the kiln tail smoke chamber is reduced to N 2 to achieve the goal of reducing NO x .
  • staged combustion schemes used are often the same, and no corresponding changes and adjustments are made according to the furnace type.
  • the inherent defects of the existing staged combustion technology lead to staged combustion.
  • the concept has been proposed for many years, in cement production, the actual NO x reduction effect is not very satisfactory, and sometimes even no effect.
  • staged combustion is a more economical NO x reduction method, but the traditional fuel/air staged combustion technology concept is still limited to the calciner body (upper, middle or lower cone) and its connection with the rotary
  • the connecting smoke chamber or flue space between the kilns creates a reducing atmosphere by creating an oxygen-deficient combustion zone to achieve NO x reduction.
  • the traditional fuel/air staged combustion technology has the following technical defects in terms of its technical characteristics:
  • the fuel is classified downwards (kiln tail flue chamber). Although the reduction time can be extended, there is a risk of pulverized coal deposits and falling into the tail of the rotary kiln along with the raw cement material.
  • the fallen coal pulverized coal is burned in the rotary kiln It is easy to cause the local temperature to be too high, cause the cement raw material to crust, reduce the quality of the cement clinker, and even cause the failure of the rotary kiln, resulting in huge production shutdown losses.
  • the fuel is graded upward (the upper part of the calciner).
  • the reducing area can be created many times, it is easy to cause incomplete combustion of the pulverized coal due to insufficient residence time of the pulverized coal, which affects the combustion efficiency, resulting in heat consumption of the entire cement production process system increase.
  • unburned coal particles are very likely to be collected by the cyclone at the outlet of the calciner and enter the tail of the rotary kiln, causing problems such as high-temperature crusting and bonding of the cement raw material, and even shutdown of the kiln.
  • a multi-stage suspension preheating cement kiln system including:
  • the decomposition furnace is connected with the smoke chamber of the rotary kiln;
  • a multi-stage suspension preheater used to preheat the raw cement material includes at least the last cyclone, the second last cyclone and the heat exchange pipes between the two, among which: smoke from the decomposition furnace The air flows into the final cyclone, and between the upper and lower cyclones of the multi-stage suspension preheater, the outlet flue gas of the lower cyclone passes through the heat exchange pipe into the upper cyclone;
  • the raw cement conveying pipeline communicates with the multi-stage suspension preheater
  • Coal feeding device used to supply coal powder to the system
  • At least one heat exchange pipe is provided with a preheater coal feed point
  • the coal feeding device is suitable for feeding pulverized coal to the multi-stage suspension preheater through the coal feeding point of the preheater.
  • the coal feeding device is also suitable for feeding pulverized coal to the calciner.
  • the coal feed point of the preheater is adjacent to the flue gas outlet of the corresponding lower cyclone.
  • the coal feed point of the preheater is arranged on the heat exchange pipe between the last-stage cyclone and the next-last-stage cyclone.
  • the amount of coal fed into the coal feeding point through the preheater is 5%-50% of the total amount of coal fed into the decomposition furnace and the heat exchange pipeline by the coal feeding device;
  • the amount of coal fed into the coal feeding point through the preheater is 20%-30% of the total amount of coal fed into the decomposition furnace and the heat exchange pipeline by the coal feeding device.
  • the cement kiln system further includes a supplemental combustion air supply device, which is used to provide supplementary combustion air to the outlet flue of the corresponding upper cyclone connected to the heat exchange pipe provided with the preheater coal feed point.
  • the supplemental combustion air is used to burn out the coal gas produced by the pyrolysis or gasification of the pulverized coal in the pipe connected to the cyclone, reducing the coal consumption of the system.
  • the cement kiln system further includes a cement raw meal temperature adjustment pipeline, which communicates with a corresponding heat exchange pipeline provided with a preheater coal feed point. Further optionally, the cement raw meal temperature adjustment pipeline is provided with a feed adjustment device.
  • the embodiment of the present invention also relates to a control method of a multi-stage suspension preheating cement kiln system
  • the cement kiln system includes: a rotary kiln with a rotary kiln smoke chamber; a decomposition furnace, which is connected to the rotary kiln smoke chamber; a multi-stage suspension preheater for preheating cement raw meal, the multi-stage suspension preheater at least includes The last-stage cyclone and the next-last-stage cyclone and the heat exchange pipes between the two, among which: the flue gas from the calciner is passed into the last-stage cyclone, and is between the upper and lower cyclones of the multi-stage suspension preheater In between, the outlet flue gas of the lower cyclone is connected to the upper cyclone through the heat exchange pipe,
  • the method includes the steps:
  • the pulverized coal is supplied to at least one heat exchange pipe, and the pulverized coal entering the heat exchange pipe is pyrolyzed or gasified in the heat exchange pipe to form coal char and coal gas.
  • supplying pulverized coal to the at least one heat exchange pipe includes the step of supplying pulverized coal to the heat exchange pipe located between the last-stage cyclone tube and the last-stage cyclone tube.
  • the amount of coal fed to the heat exchange pipe is 5%-50% of the total amount of coal fed to the calciner and the heat exchange pipe;
  • the amount of coal fed to the heat exchange pipe is 20%-30% of the total amount of coal fed to the calciner and the heat exchange pipe.
  • the method further includes the step of: providing supplementary combustion air to the outlet flue of the corresponding upper cyclone connected to the heat exchange pipe for the coal.
  • the supplemental combustion air is used to burn out the coal gas produced by the pyrolysis or gasification of the pulverized coal in the pipe connected to the cyclone, reducing the coal consumption of the system.
  • the method further includes the step of passing cement raw meal into the heat exchange pipe for feeding coal to adjust the temperature change caused by the feeding of coal powder.
  • the embodiment of the present invention also relates to a control method of a multi-stage suspension preheating cement kiln system
  • the cement kiln system includes: a rotary kiln with a rotary kiln smoke chamber; a decomposition furnace, which is connected to the rotary kiln smoke chamber; a multi-stage suspension preheater for preheating cement raw meal, the multi-stage suspension preheater at least includes The last-stage cyclone, the next-last-stage cyclone and the heat exchange pipes between the two, among which: the flue gas from the decomposition furnace is passed into the last-stage cyclone, and it is between the upper and lower cyclones of the multi-stage suspension preheater. In between, the outlet flue gas of the lower cyclone is connected to the upper cyclone through the heat exchange pipe,
  • the method includes the steps:
  • the at least one heat exchange pipe is supplied with pulverized coal so that the upper cyclone corresponding to the heat exchange pipe is in a reducing atmosphere.
  • Fig. 1 is a schematic diagram of a multi-stage suspension preheating cement kiln system according to an exemplary embodiment of the present invention.
  • Fig. 2 is a schematic diagram of a multi-stage suspension preheating cement kiln system according to another exemplary embodiment of the present invention.
  • Fig. 1 is a schematic diagram of a multi-stage suspension preheating cement kiln system according to an exemplary embodiment of the present invention.
  • a multi-stage suspension preheating cement kiln system includes:
  • the rotary kiln 10 has a rotary kiln smoke chamber 20;
  • the decomposition furnace 30 is connected with the smoke chamber 20 of the rotary kiln;
  • a multi-stage suspension preheater used to preheat the cement raw meal at least includes the last-stage cyclone drum 41, the next-last-stage cyclone drum 42 and the heat exchange pipe L1 between the two.
  • the example of FIG. 1 includes 5 levels of cyclones 41 to 45, among which there are two primary cyclones 45.
  • the flue gas from the calciner 30 is passed into the final cyclone 41 (five-stage cyclone), and the outlet flue gas is passed through the heat exchange pipe L1 to the next-end cyclone 42 (four-stage cyclone); from the top of the cyclone 42
  • the discharged outlet flue gas is passed into the third-stage cyclone 43 through the heat exchange pipe L2, and the preheated raw meal discharged from the cyclone 43 passes through the discharge pipe to L1; the outlet flue gas of the cyclone 43 passes through L3.
  • the discharge pipe of the cyclone cylinder 44 is connected to L2, and the other is the same.
  • the raw cement conveying pipe L6 is connected to the primary cyclone 45.
  • At least one heat exchange pipe is provided with a preheater coal feed point (the preheater coal feed point 411 in the figure), and the coal feeder 50 supplies pulverized coal to the multi-stage cyclone preheater through the preheater coal feed point.
  • the coal feeding device 50 also supplies pulverized coal to the calciner through the coal feeding point on the calciner 31.
  • the cyclone that first enters from the raw cement conveying pipe is the primary cyclone.
  • the upper and lower stages of the cyclone in the multi-stage suspension preheater are opposite to the flow direction of the flue gas: the downstream in the flue gas flow direction is the upper cyclone, and the upstream is the lower cyclone.
  • the cyclone at the most upstream of the flue gas flow direction is the last cyclone, and the cyclone at the downstream of the last cyclone is the second last cyclone.
  • the specific location of the coal feed point of the preheater on the specific heat exchange pipe is adjacent to the flue gas outlet of the corresponding lower cyclone, and relatively far away from the inlet of the upper cyclone, as shown in Figure 1 411 is adjacent to the flue gas outlet of the cyclone 41 and far away from the cyclone 42.
  • the residence time of pulverized coal in the heat exchange pipeline is longer, and the preheating is more sufficient.
  • the preheater coal feed point 411 is set on the heat exchange pipe L1 between the final cyclone 41 and the next final cyclone 42. It should be pointed out that the coal feed point of the preheater is not limited to being set on the heat exchange pipe of the flue gas outlet of the final cyclone. As long as the temperature is appropriate, the coal feed point of the preheater can be located in the secondary cyclone 44 and the third cyclone 43. Or on the outlet heat exchange pipe of the fourth-stage cyclone (the last-stage cyclone) 42.
  • the preheater coal feed point is not limited to single point coal feed, and multiple preheaters can also be set up at the same time in the heat exchange pipes of the flue gas outlet of the cyclone tube at all levels (except the primary cyclone tube 45). Point, forming a combined high-level coal feed, multi-stage enhanced NO x reduction.
  • the coal feeding amount of the coal feeding device to the heat exchange pipeline is 5%-50% of the total coal feeding amount that the coal feeding device adds to the calciner and the heat exchange pipeline, for example, 5%, 15% , 35%, 50%;
  • the amount of coal fed by the coal feeding device to the heat exchange pipe is 20%-30% of the total amount of coal fed by the coal feeding device to the calciner and the heat exchange pipe, for example 20%, 25%, 30%.
  • the cement kiln system may also include a supplementary combustion air inlet 421 arranged at the outlet of the cyclone tube 42 for connecting to the heat exchange pipe of the upper-level cyclone tube 42 connected to the heat exchange pipe L1 of the coal supply.
  • a supplementary combustion air inlet 421 arranged at the outlet of the cyclone tube 42 for connecting to the heat exchange pipe of the upper-level cyclone tube 42 connected to the heat exchange pipe L1 of the coal supply.
  • the supplemental combustion air is used to burn off the coal gas produced by the pyrolysis or gasification of the pulverized coal in the heat exchange pipe L1 to reduce the coal consumption of the system.
  • the supplementary combustion air may not be provided.
  • the preheater on L1 feeds the coal point 411.
  • the tertiary air is fed in from the tertiary tuyere 32 and the tertiary tuyere 33 on the calciner to ensure that the coal fed to the calciner is burned out.
  • the tertiary tuyere 32 is located above the coal feeding point 31 of the calciner and on the straight cylinder section of the calciner.
  • the high NO x concentration kiln gas from the rotary kiln 10 enters the bottom of the decomposition furnace 30 through the flue chamber 20, and the spray effect produced by the bottom necking makes the flue gas and the pulverized coal particles fully mixed, and the pulverized coal particles are simultaneously preheated , Forming high-temperature coal char and gas with reducing effect, the area between the bottom of the decomposition furnace and the tertiary tuyere 32 is a strong reduction area, and the NO x in the kiln gas is reduced.
  • the area between the tertiary tuyere 32 and the tertiary tuyere 33 is a weak reduction area, and the reduction intensity of NO x is weakened.
  • Three or more outlet region 33 is oxidized region, reduction of NO x disappears, and the flue gas still contains a substantial NO x reduction is not and / or the precalciner combustion. After this part of the flue gas comes out of the five-stage cyclone 41, it still has a high temperature of, for example, about 850°C.
  • the pulverized coal fed to the coal point 411 of the preheater will be preheated, and the pulverized coal will be pyrolyzed or gasified.
  • the coke and coal gas will form a strong reducing atmosphere in the heat exchange pipe L1 and the internal area of the fourth-stage cyclone 42 to reduce the NO x in the flue gas again.
  • Four cyclone 42 may extend the contact time of the flue gas with the reducing coal / gas, resulting in improved NO x reduction efficiency.
  • the coal gas that has not participated in the reduction reaction flows out from the outlet of the fourth-stage cyclone 42 along with the flue gas.
  • the heat exchange pipe at the outlet of the fourth-stage cyclone 42 is provided with a supplementary combustion air inlet position 421 where the remaining gas will be burned.
  • the high-temperature coal char is separated by the four-stage cyclone 42 and returned to the calciner together with the cement raw meal to provide heat for the endothermic decomposition reaction of the cement raw meal.
  • the lower outlet of the last cyclone drum 42 communicates with the decomposition furnace 30; and the lower outlet of the last cyclone drum 41 communicates with the rotary kiln 10.
  • the position of the coal feed point 31 of the calciner can be adjusted, and it is not limited to single-point coal feed, and the tertiary air is not limited to single-point air distribution.
  • the tertiary air can be adjusted accordingly according to the specific number and location of coal feed points in the calciner. The number and location of the distribution points to ensure fuel burnout and reduce coal consumption in the system.
  • the cement kiln system according to the present invention may further include: a tertiary tuyere arranged on the calciner; and a tertiary air supply control device, which is suitable for controlling the air volume of the tertiary air, A reducing atmosphere is formed below the tertiary tuyere, and a non-reducing atmosphere is formed above the tertiary tuyere.
  • the tertiary tuyere includes a first tertiary tuyere and a second tertiary tuyere arranged on the calciner at intervals in the vertical direction; a tertiary air supply control device is suitable for controlling the air volume of the tertiary air to A first reducing atmosphere is formed between the bottom of the calciner and the first tertiary tuyere, and a second reducing atmosphere weaker than the first reducing atmosphere is formed between the first tertiary tuyere and the second tertiary tuyere, and the A non-reducing atmosphere is formed above the secondary and tertiary tuyere.
  • the embodiment of the present invention also proposes a control method of the above-mentioned multi-stage suspension preheating cement kiln system, which includes the steps of: supplying pulverized coal to at least one heat exchange pipe, and the pulverized coal entering the heat exchange pipe is exchanging heat.
  • the pipeline is pyrolyzed or gasified to form coal char and gas.
  • supplying pulverized coal to the at least one heat exchange pipe includes the step of supplying pulverized coal to the coal feed point of the heat exchange pipe corresponding to the flue gas outlet of the lower cyclone.
  • supplying pulverized coal to the at least one heat exchange pipe includes the step of supplying pulverized coal to the heat exchange pipe located between the last-stage cyclone tube and the last-stage cyclone tube.
  • the amount of coal supplied to the heat exchange pipeline is 5%-50% of the total amount of coal supplied to the calciner and the heat exchange pipeline; in a further embodiment, the coal supply to the heat exchange pipeline The amount is 20%-30% of the total coal supply to the calciner and heat exchange pipeline.
  • the method further includes the step of: providing supplementary combustion air to the outlet flue of the upper cyclone connected to the heat exchange pipe fed to the coal.
  • the embodiment of the present invention also relates to a control method of a multi-stage suspension preheating cement kiln system.
  • the cement kiln system includes: a rotary kiln; a decomposition furnace, which is connected to the rotary kiln smoke chamber; and is used for preheating cement raw meal.
  • the multi-stage suspension preheater includes at least the last-stage cyclone, the last-stage cyclone and the heat exchange pipes between the two. Among them: the flue gas from the decomposition furnace is passed into the last-stage cyclone , And between the upper and lower cyclones of the multi-stage suspension preheater, the outlet flue gas of the lower cyclone is passed into the upper cyclone through the heat exchange pipe.
  • the method includes the step of: supplying coal to at least one heat exchange pipe Powder, so that the upper cyclone corresponding to the heat exchange pipe is in a reducing atmosphere.
  • Fig. 2 is a schematic diagram of an exemplary embodiment of a multi-stage suspension preheating cement kiln system with temperature adjustment provided by the present invention.
  • a multi-stage suspension preheating cement kiln system with temperature adjustment in addition to the features of the embodiment shown in Figure 1, also includes:
  • the pipe tee 71 is used for the distribution of cement raw meal.
  • the pipe tee 71 has a first outlet and a second outlet;
  • Cement raw meal temperature adjustment pipeline L5 used to transport cement raw meal participating in temperature adjustment, one end of which is connected to the first outlet, and the other end is connected to the heat exchange after the coal feed point of the preheater at the outlet of the final cyclone 41
  • the pipeline L1 and the cement raw meal temperature control pipeline L5 are provided with a gate valve 72 and an air lock valve 73, the gate valve is used to control the flow of the cement raw material involved in temperature regulation, and the air lock valve 73 is used to seal the system; and
  • the raw cement conveying pipe L6 has one end connected to the second outlet of the pipe tee 71, and the other end connected to the preheating flue gas communication pipe L4 at the outlet of the secondary cyclone 44.
  • the air lock valve is a valve that can automatically open after a certain weight and close when the weight is less than that to ensure the sealing of the system.
  • the feed of the air lock valve is intermittent in the microscopic view, but can be regarded as continuous in the macroscopic view (step feeding with short time interval).
  • other sealing devices that maintain a negative pressure state can also be used, all of which fall within the protection scope of the present invention.
  • the gate valve 72 and the air lock valve 73 are provided separately, they may also be provided as a single body.
  • connection point between the cement raw meal temperature regulating pipe L5 and the heat exchange pipe L1 at the outlet of the final cyclone 41 is after the preheater coal feed point 411 (downstream determined by the flue gas flow direction), which is higher than the preheater coal feed Point closer to the superior cyclone.
  • the embodiment of the present invention also proposes a temperature control method for a multi-stage suspension preheating cement kiln system, which includes the steps of: supplying pulverized coal to at least one heat exchange pipe, and the pulverized coal entering the heat exchange pipe is exchanging heat
  • the pipeline is pyrolyzed or gasified to form coal char and coal gas; the coal char and coal gas formed by pyrolysis or gasification is passed cement raw meal to participate in temperature control.
  • the temperature control method of the multi-stage suspension preheating cement kiln system will be specifically described below with reference to FIG. 2.
  • the three-way pipe 71 divides the normal temperature cement raw material conveyed by the hoist into two paths, and the raw cement material passes through the cement raw material conveying pipe L6 into the outlet of the cyclone 44 for heat exchange.
  • the pipe L4 is heated by the flue gas and brought into the cyclone separator 45; the other cement raw material passes through the cement raw material temperature control pipe L5, passes through the gate valve 72 and the air lock valve 73 in turn, and enters the outlet heat exchange pipe of the cyclone separator 41 L1, the specific feeding position is downstream of the coal feed point 411 of the preheater. Since the heat exchange pipe L1 is in a negative pressure state, an air lock valve 73 is provided on the cement raw material temperature control pipe L5 to prevent air from leaking into the heat exchange pipe L1. In the actual cement process, the flue gas at the outlet of the cyclone 41 contains a certain amount of oxygen.
  • the pulverized coal After the pulverized coal is fed from the coal feed point 411 of the preheater, part of the pulverized coal will be burned, which will cause the flue gas temperature to rise and pass into the normal temperature cement production. After mixing, the temperature of the flue gas can be effectively reduced to prevent the preheating system from skinning due to overheating (generally, the cement raw meal is prone to skinning when it exceeds 1000°C).
  • the opening degree of the gate valve 72 By controlling the opening degree of the gate valve 72, the flow rate of the cement raw meal participating in temperature adjustment can be adjusted, so that the flue gas temperature can be reasonably adjusted and controlled.
  • the cement raw meal that participates in temperature adjustment and the cement raw meal collected by the cyclone tube 43 are combined, and then enter the cyclone separator 42 and finally enter the decomposition furnace 30.
  • coal feeding device can supply other fuels that can achieve technical purposes, such as biomass fuel, all of which are within the protection scope of the present invention.
  • the coal is reduced by setting the point on the preheater flue gas outlet duct of cyclone exhaust NO x in principle simple and easy to implement, less impact on the existing cement production process, transformation of low cost.
  • the idea of high-level fuel classification is used instead of the traditional fuel-staged combustion technology to feed coal in the flue chamber, which avoids the risk of coal particles falling into the tail of the rotary kiln and causing over-temperature skinning in a local area of the rotary kiln .
  • the pulverized coal fed into the multi-stage suspension preheater will eventually return to the calciner for combustion, providing heat for the decomposition of the cement raw meal, and avoiding the incombustibility of the pulverized coal caused by the upward fuel classification. Complete question. Therefore, the present invention does not significantly increase the coal consumption (heat consumption) of the system while realizing the efficient reduction of NO x in the flue gas, and effectively controls the operating cost.
  • the “coal feeding device” in the claims of the present invention also includes a device suitable for use in cement kilns in addition to the coal feeding device.
  • the "pulverized coal” in the claims of the present invention also includes other fuel forms suitable for use in cement kilns in addition to fuel in the form of pulverized coal.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Ceramic Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Furnace Details (AREA)

Abstract

一种多级悬浮预热水泥窑炉系统和多级悬浮预热水泥窑炉系统的控制方法，多级悬浮预热水泥窑炉系统包括：回转窑，具有回转窑烟室；分解炉，与回转窑烟室连通；用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒、次末级旋风筒及两者之间的换热管道，其中：来自分解炉的烟气通入末级旋风筒，且在多级悬浮预热器的上下两级旋风筒之间，下级旋风筒的出口烟气通过换热管道通入上级旋风筒；水泥生料输送管道，与多级悬浮预热器相通；和给煤装置，用于向系统供给煤粉，其中：至少一个换热管道上设有预热器给煤点；给煤装置适于通过预热器给煤点向多级悬浮预热器供给煤粉。

Description

多级悬浮预热水泥窑炉系统及其控制方法 技术领域
本发明的实施例涉及水泥工业氮氧化物排放控制领域，尤其涉及一种多级悬浮预热水泥窑炉系统及其控制方法。
背景技术
目前，国内外普遍采用的水泥生产工艺为新型干法水泥生产工艺，其中回转窑和分解炉是其工艺环节中的主要设备。
回转窑是水泥熟料最终烧成装置，由于窑内为气固堆积式传热，传热效果较差，为了得到高质量水泥熟料，窑头煅烧气体温度高达1800℃，这造成回转窑热力型NO x排放极高，占到所有热力型NO x排放的80％以上。而且，鉴于回转窑高温煅烧工艺的特点，此部分热力型NO x的生成无法避免。
分解炉是水泥生料分解装置，水泥生料在分解炉内分解需要吸收大量热量，这部分热量依靠煤粉燃烧提供，因此分解炉内燃烧需要的给煤量高于回转窑燃烧所需的给煤量(占所有给煤量的60％左右)，使得分解炉内的燃料型NO x排放较高。
回转窑和分解炉是目前新型干法水泥生产工艺NO x排放的两大主要来源，造成水泥窑炉总体NO x排放处于较高水平，原始排放超过1000mg/Nm 3。统计数据显示，水泥工业2017年的NO x排放量占到了全国NO x排放总量的10-12％，是我国雾霾天气的重要成因之一，严重危害大气环境和人类健康。由此可见，实现水泥窑炉低NO x排放对于大气污染治理具有重要战略意义。
我国水泥工业NO x排放标准(GB4915-2013)规定，重点地区NO x排放控制水平不高于320mg/Nm 3，一般地区不高于400mg/Nm 3，一些地方省市地区甚至提出了更高的排放标准。比如江苏省规定水泥工业2019年6月1日前NO x排放不能高于100mg/Nm 3；河南省规定2018年10月 前，改造后的水泥企业在基准氧含量10％条件下NO x浓度不高于150mg/Nm 3。
为了满足日益严苛的排放标准，目前大多数水泥企业不得不在分解炉尾部采用选择性非催化还原(SNCR)脱硝技术，即以氨水为还原剂还原NO x，这不仅使得水泥附加成本增加，同时存在氨逃逸，从而带来新的环境污染问题。
除了SNCR技术以外，分解炉燃料/空气分级燃烧技术也一直受到水泥企业的重视。分级燃烧技术，是将分解炉所用煤粉燃料或者燃料燃烧所用的空气进行分级多点配送，在保证燃料燃烧效率的情况下尽可能多的营造出还原性气氛区域，一方面降低NO x的生成，另一方面将来自窑尾烟室中的NO x还原成N 2，以达到NO x减排的目的。
不过，由于不同的水泥分解炉在结构上存在很大差异，而采用的分级燃烧方案往往千篇一律，没有根据炉型做出相应改变和调整，加之现有分级燃烧技术存在的固有缺陷，导致分级燃烧概念虽已提出多年，但在水泥生产中，实际NO x减排效果却不甚理想，有时候甚至没有效果。
对于干法水泥生产工艺而言，分级燃烧是较为经济的NO x减排方法，但是传统的燃料/空气分级燃烧技术概念仍然局限于分解炉本体(上部、中部或者下部锥体)及其与回转窑之间的连接烟室或烟道空间，通过营造缺氧燃烧区域构建还原气氛，从而实现NO x还原。
传统的燃料/空气分级燃烧技术，从其技术特征来看，主要存在以下技术缺陷：
(1)燃料向下(窑尾烟室)分级，虽然可以延长还原时间，但存在煤粉沉积、随水泥生料一起落入到回转窑尾部的风险，落入的煤粉在回转窑内燃烧易造成局部温度过高，引起水泥生料结皮粘结，降低了水泥熟料质量，甚至引起回转窑故障，造成巨大的停产损失。
(2)燃料向上(分解炉上部)分级，虽然可以多次营造还原性区域，但是容易因为煤粉停留时间不够，造成煤粉燃烧不完全，影响燃烧效率，从而导致整个水泥生产工艺系统热耗增加。另外，未燃尽的煤粉颗粒极有可能被分解炉出口旋风筒收集，从而进入回转窑尾部，造成水泥生料高温 结皮粘结、甚至停窑的问题。
发明内容
为缓解或解决上述问题中的至少一个方面或者至少一点，提出本发明。
根据本发明的实施例的一个方面，提出了一种多级悬浮预热水泥窑炉系统，包括：
回转窑，具有回转窑烟室；
分解炉，与回转窑烟室连通；
用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒、次末级旋风筒及两者之间的换热管道，其中：来自分解炉的烟气通入末级旋风筒，且在多级悬浮预热器的上下两级旋风筒之间，下级旋风筒的出口烟气通过换热管道通入上级旋风筒；
水泥生料输送管道，与多级悬浮预热器相通；和
给煤装置，用于向系统供给煤粉；
其中：
至少一个换热管道上设有预热器给煤点；
所述给煤装置适于通过所述预热器给煤点向多级悬浮预热器供给煤粉。
可选的，所述给煤装置还适于向分解炉供给煤粉。
可选的，所述预热器给煤点邻近对应的下级旋风筒的烟气出口。
可选的，所述预热器给煤点设置于末级旋风筒与次末级旋风筒之间的换热管道上。
可选的，通过所述预热器给煤点加入的给煤量为所述给煤装置向分解炉和换热管道加入的总给煤量的5％-50％；
可选的，通过所述预热器给煤点加入的给煤量为所述给煤装置向分解炉和换热管道加入的总给煤量的20％-30％。
可选的，水泥窑炉系统还包括补燃风供给装置，用于向与设有预热器给煤点的换热管道相连的对应上级旋风筒的出口烟道提供补燃风。该补燃风用于将旋风筒连通管道内煤粉热解或者气化产生的煤气燃尽，减小系统 煤耗。
可选的，所述水泥窑系统还包括水泥生料调温管道，其与设有预热器给煤点的相应换热管道相通。进一步可选的，所述水泥生料调温管道设置有给料调节装置。
本发明的实施例还涉及一种多级悬浮预热水泥窑炉系统的控制方法，
所述水泥窑炉系统包括：回转窑，具有回转窑烟室；分解炉，与回转窑烟室连通；用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒与次末级旋风筒及两者之间的换热管道，其中：来自分解炉的烟气通入末级旋风筒，且在多级悬浮预热器的上下两级旋风筒之间，下级旋风筒的出口烟气通过换热管道连通到上级旋风筒，
所述方法包括步骤：
向至少一个换热管道供给煤粉，进入所述换热管道的煤粉在换热管道内被热解或者气化而形成煤焦和煤气。
可选的，向至少一个换热管道供给煤粉包括步骤：向位于末级旋风筒以及次末级旋风筒之间的换热管道供给煤粉。
可选的，向所述换热管道的给煤量为向分解炉和换热管道加入的总给煤量的5％-50％；
可选的，向所述换热管道的给煤量为向分解炉和换热管道加入的总给煤量的20％-30％。
可选的，所述方法还包括步骤：向与给煤的换热管道相连的对应上级旋风筒的出口烟道提供补燃风。该补燃风用于将旋风筒连通管道内煤粉热解或者气化产生的煤气燃尽，减小系统煤耗。进一步的，所述方法还包括步骤：向所述给煤的换热管道中通入水泥生料，以调节由于煤粉给入引起的温度变化。
本发明的实施例还涉及一种多级悬浮预热水泥窑炉系统的控制方法，
所述水泥窑炉系统包括：回转窑，具有回转窑烟室；分解炉，与回转窑烟室连通；用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒、次末级旋风筒及两者之间的换热管道，其中：来自分解炉的烟气通入末级旋风筒，且在多级悬浮预热器的上下两级旋风筒之间，下级旋风筒的出口烟气通过换热管道连通到上级旋风筒，
所述方法包括步骤：
向至少一个换热管道供给煤粉，使得与该换热管道对应的上级旋风筒内处于还原性气氛。
附图说明
图1为根据本发明的一个示例性实施例的多级悬浮预热水泥窑炉系统的示意图。
图2为根据本发明的另一个示例性实施例的多级悬浮预热水泥窑炉系统的示意图。
具体实施方式
下述参照附图对本发明实施方式的说明旨在对本发明的总体发明构思进行解释，而不应当理解为对本发明的一种限制。
图1为根据本发明的一个示例性实施例的多级悬浮预热水泥窑炉系统的示意图。如图1所示，一种多级悬浮预热水泥窑炉系统包括：
回转窑10，具有回转窑烟室20；
分解炉30，与回转窑烟室20连通；
用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒41、次末级旋风筒42及两者之间的换热管道L1。图1的示例中包括旋风筒41～45共5级，其中初级旋风筒45为两个。来自分解炉30的烟气通入末级旋风筒41(五级旋风筒)，出口烟气通过换热管道L1通入到次末级旋风筒42(四级旋风筒)；从旋风筒42顶部排出的出口烟气通过换热管道L2通入到第3级旋风筒43，旋风筒43排出的预热后的生料通过排料管通入到L1；旋风筒43的出口烟气通过L3通入到旋风筒44，旋风筒44的排料管连通到L2，其他同理。水泥生料输送管L6连通到初级旋风筒45。
至少一个换热管道上设有预热器给煤点(如图中的预热器给煤点411)，给煤装置50通过预热器给煤点向多级旋风预热器供给煤粉。
可选的，给煤装置50还通过分解炉31上的给煤点向分解炉供给煤粉。
在本发明中，自水泥生料输送管首先进入的旋风筒为初级旋风筒。初级旋风筒可以为一个，也可以为并行设置的多个。
在本发明中，多级悬浮预热器中旋风筒的上级与下级，与烟气的流动方向相反：处于烟气流动方向下游的，为上级旋风筒，而处于上游的，为下级旋风筒，处于烟气流动方向最上游的旋风筒为末级旋风筒，处于末级旋风筒下游的旋风筒为次末级旋风筒。
优选的，预热器给煤点在特定换热管道上的具体位置邻近对应的下级旋风筒的烟气出口，而相对远离上级旋风筒入口，如图1中示出的预热器给煤点411邻近旋风筒41的烟气出口、远离旋风筒42。这样煤粉在换热管道中的停留时间较长，预热更加充分。
在如图1所示的示例中，预热器给煤点411设置于末级旋风筒41与次末级旋风筒42之间的换热管道L1上。需要指出的是，预热器给煤点不仅限于设置于末级旋风筒烟气出口换热管道上，只要温度合适，预热器给煤点可以位于二级旋风筒44、三级旋风筒43或者是四级旋风筒(次末级旋风筒)42的出口换热管道上。此外，在温度允许条件下，预热器给煤点不仅限于单点给煤，还可以在各级旋风筒烟气出口换热管道(初级旋风筒45除外)同时设置多个预热器给煤点，形成组合式高位给煤，多级强化NO x还原。
可选的，所述给煤装置向换热管道的给煤量为所述给煤装置向分解炉和换热管道加入的总给煤量的5％-50％，例如，5％、15％、35％、50％；进一步的实施例中，所述给煤装置向换热管道给煤量为给煤装置向分解炉和换热管道加入的总给煤量的20％-30％，例如20％、25％、30％。
如图1所示，水泥窑炉系统还可包括设置在旋风筒42出口的补燃风加入口421，用于向与给煤的换热管道L1相连的对应上级旋风筒42的出口换热管道提供补燃风。补燃风用于将换热管道L1内煤粉热解或者气化产生的煤气燃尽，减小系统煤耗，本发明中，也可以不设置补燃风。
如本领域技术人员能够理解的，在向换热管道的给煤点变化的情况下，补燃风的位置也做相应的变化。
下面参照图1，具体说明根据本发明的实施例的多级悬浮预热水泥窑炉系统降低NO x排放的实施步骤。
将整个系统除回转窑外的给煤分成两部分，一部分从分解炉底部锥体上的分解炉给煤点31给入，另一部分从五级旋风筒(末级旋风筒)41出口换热管道L1上的预热器给煤点411给入。三次风从分解炉上的三次风口32和三次风口33给入，确保分解炉给煤的燃尽，其中三次风口32位于分解炉给煤点31的上方且处于分解炉的直筒段上，三次风口33位于分解炉中部喷腾缩口上方附近，以便于通过喷腾效应强化气固掺混。来自回转窑10的高NO x浓度窑气通过烟室20进入分解炉30的底部，并且通过底部缩口产生的喷腾效应使得烟气和煤粉颗粒充分掺混，煤粉颗粒同时被预热，形成具有还原作用的高温煤焦和煤气，分解炉底部至三次风口32之间的区域为强还原区域，窑气中的NO x被还原。三次风口32与三次风口33之间的区域为弱还原区域，NO x的还原强度减弱。三次风口33以上的区域为氧化性区域，NO x还原作用消失，此时烟气中仍然含有大量未被还原和/或分解炉燃烧产生的NO x。这部分烟气从五级旋风筒41出来以后，仍然具有例如850℃左右的高温，将对预热器给煤点411给入的煤粉进行预热，煤粉热解或者气化形成的煤焦和煤气将在换热管道L1以及四级旋风筒42内部区域内形成强还原性气氛，从而对烟气中的NO x进行再次还原。四级旋风筒42可以延长烟气与还原性煤焦/煤气的接触时间，从而大幅提高NO x还原效率。未参与还原反应的煤气随烟气从四级旋风筒42出口流出，在四级旋风筒42出口换热管道上设置有补燃风通入口位置421，剩余的煤气将在此处燃烧。高温煤焦则被四级旋风筒42分离下来，并且与水泥生料一起返回分解炉燃烧，为水泥生料吸热分解反应提供热量。
基于以上，在可选的实施例中，如图1所示，次末级旋风筒42的下部出口与分解炉30连通；且末级旋风筒41的下部出口与回转窑10相通。
需要指出的是，分解炉给煤点31的位置可调整，且不仅限于单点给煤，三次风也不仅限于单点配风，可根据分解炉具体给煤点数目和位置，相应调整三次风的配送点数和位置，以确保燃料的燃尽，降低系统煤耗。
基于以上，在可选的实施例中，根据本发明的水泥窑炉系统还可以包括：设置在分解炉上的三次风口；以及三次风供风控制装置，适于控制三次风的风量，以在三次风口下方形成还原性气氛，且在三次风口上方形成非还原性气氛。进一步的，所述三次风口包括在竖直方向上间隔开设置在 分解炉上的第一三次风口和第二三次风口；三次风供风控制装置，适于控制三次风的风量，以在分解炉底部与第一三次风口之间形成第一还原性气氛，在第一三次风口与第二三次风口之间形成弱于第一还原性气氛的第二还原性气氛，且在第二三次风口上方形成非还原性气氛。
基于以上，本发明的实施例也提出了一种上述多级悬浮预热水泥窑炉系统的控制方法，包括步骤：向至少一个换热管道供给煤粉，进入换热管道的煤粉在换热管道内被热解或者气化而形成煤焦和煤气。
可选的，向至少一个换热管道供给煤粉包括步骤：向换热管道的对应下级旋风筒的烟气出口的给煤点供给煤粉。
可选的，向至少一个换热管道供给煤粉包括步骤：向位于末级旋风筒以及次末级旋风筒之间的换热管道供给煤粉。
可选的，向所述换热管道的给煤量为向分解炉和换热管道供给的总煤量的5％-50％；在进一步的实施例中，向所述换热管道的给煤量为向分解炉和换热管道供给的总给煤量的20％-30％。
可选的，所述方法还包括步骤：向与被给煤的换热管道相连的上级旋风筒的出口烟道提供补燃风。
本发明的实施例还涉及一种多级悬浮预热水泥窑炉系统的控制方法，所述水泥窑炉系统包括：回转窑；分解炉，与回转窑烟室连通；用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒、次末级旋风筒及两者之间的换热管道，其中：来自分解炉的烟气通入末级旋风筒，且在多级悬浮预热器的上下两级旋风筒之间，下级旋风筒的出口烟气通过换热管道通入到上级旋风筒，所述方法包括步骤：向至少一个换热管道供给煤粉，使得与该换热管道对应的上级旋风筒内处于还原性气氛。
图2所示为本发明提供的一种带温度调节的多级悬浮预热水泥窑炉系统的示例性实施例示意图。如图2所示，一种带温度调节的多级悬浮预热水泥窑炉系统，除了具有图1中所示的实施例的特征以外，还包括：
管道三通71，用于水泥生料的分配，管道三通71具有第一出口和第二出口；
水泥生料调温管道L5，用于输送参与温度调节的水泥生料，其一端连通到所述第一出口，另一端连接到末级旋风筒41出口的预热器给煤点 之后的换热管道L1，且水泥生料调温管道L5设置有闸阀72和锁风阀73，闸阀用于控制参与温度调节的水泥生料的流量，锁风阀73用于系统的密封；和
水泥生料输送管道L6，在可选的实施例中，其一端连接在管道三通71的第二出口，另一端连接到二级旋风筒44出口的预热烟气连通管道L4。
由于管道L1中是负压状态，因此需要防止管道L5进入空气，锁风阀是一种可以到一定重量后自动打开，小于该重量时关闭的阀门，保证系统的密封。锁风阀给料在微观上是间断的，但在宏观上可认为是连续的(时间间隔很短的阶跃给料)。除了锁风阀之外，还可以采用其他保持负压状态的密封装置，均在本发明的保护范围之内。
在图2中，虽然闸阀72与锁风阀73分开设置，但是，两者也可以为一体设置。
所述水泥生料调温管道L5与末级旋风筒41出口的换热管道L1的连通点在预热器给煤点411之后(以烟气流动方向确定的下游)，较预热器给煤点更靠近上级旋风筒。
基于以上，本发明的实施例也提出了一种多级悬浮预热水泥窑炉系统的温度控制方法，包括步骤：向至少一个换热管道供给煤粉，进入换热管道的煤粉在换热管道内被热解或者气化而形成煤焦和煤气；向热解或者气化形成的煤焦和煤气中通入水泥生料，参与温度控制。
下面参照图2具体说明根据本发明的实施例的多级悬浮预热水泥窑炉系统的温度控制方法。在图2所示的示例中，所述的管道三通71将提升机输送过来的常温水泥生料分成两路，一路水泥生料通过水泥生料输送管道L6进入旋风分离器44的出口换热管道L4,并被烟气加热后带入旋风分离器45；另一路水泥生料通过水泥生料调温管道L5依次经过闸阀72和锁风阀73后，进入旋风分离器41的出口换热管道L1，具体的进料位置在预热器给煤点411的下游。由于换热管道L1内为负压状态，故在水泥生料调温管道L5上设置锁风阀73，防止空气泄露进入换热管道L1。在实际水泥工艺中，旋风筒41出口烟气中含有一定氧气，从预热器给煤点411给入煤粉后，将有部分煤粉燃烧，从而引起烟气温度上升，通入常 温水泥生料后，可以有效降低烟气温度，避免预热系统因为超温而结皮(一般的，水泥生料在超过1000℃时容易发生结皮现象)。通过控制闸阀72的开度可以调整参与温度调节的水泥生料的流量，从而对烟气温度进行合理的调节与控制。参与温度调节的水泥生料与旋风筒43收集下来的水泥生料汇合后，进入旋风分离器42，最终进入分解炉30内。
需要指出的是，在本发明中，虽然采用了给煤装置的表述，但是，如本领域技术人员能够理解的，给煤装置可以供给能够实现技术目的的其他燃料，例如生物质燃料，这些均在本发明的保护范围之内。
在本发明中，通过在旋风筒的烟气出口管道上设置预热器给煤点来降低NO x排放，原理简单，也容易实施，对现有水泥生产工艺影响较小，改造成本低。
在本发明中，采用燃料高位分级的思路，代替了传统燃料分级燃烧技术采用在烟室给煤的方法，避免了煤粉颗粒落入回转窑尾部，引起回转窑局部区域超温结皮的风险。
此外，在本发明中，在多级悬浮预热器给入的煤粉，最终会回到分解炉内燃烧，为水泥生料的分解提供热量，避免了燃料向上分级带来的煤粉燃烧不完全的问题。因此，本发明在实现烟气中NO x高效还原的同时，并没有明显增加系统煤耗(热耗)，有效控制了运行成本。
需要指出的是，虽然在具体实施例以煤粉为燃料为例进行了说明，但是，本发明的权利要求中“给煤装置”除了给煤装置之外还包括了适于水泥窑炉使用的其他燃料，相应的，本发明的权利要求中的“煤粉”除了煤粉形式的燃料之外也包括了适于水泥窑炉使用的其他燃料形式。
尽管已经示出和描述了本发明的实施例，对于本领域的普通技术人员而言，可以理解在不脱离本发明的原理和精神的情况下可以对这些实施例进行变化、要素组合，本发明的范围由所附权利要求及其等同物限定。

Claims (16)

  1. 一种多级悬浮预热水泥窑炉系统，包括：
    回转窑，具有回转窑烟室；
    分解炉，与回转窑烟室连通；
    用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒、次末级旋风筒及两者之间的换热管道，其中：来自分解炉的烟气通入末级旋风筒，且在多级悬浮预热器的上下两级旋风筒之间，下级旋风筒的出口烟气通过换热管道通入上级旋风筒；
    水泥生料输送管道，与多级悬浮预热器相通；和
    给煤装置，用于向系统供给煤粉；
    其中：
    至少一个换热管道上设有预热器给煤点；
    所述给煤装置适于通过所述预热器给煤点向多级悬浮预热器供给煤粉。
  2. 根据权利要求1所述的水泥窑炉系统，其中：
    所述给煤装置还适于向分解炉供给煤粉。
  3. 根据权利要求1所述的水泥窑炉系统，其中：
    所述预热器给煤点邻近对应的下级旋风筒的烟气出口。
  4. 根据权利要求1所述的水泥窑炉系统，其中：
    所述预热器给煤点设置于末级旋风筒与次末级旋风筒之间的换热管道上。
  5. 根据权利要求2所述的水泥窑炉系统，其中：
    通过所述预热器给煤点加入的给煤量为所述给煤装置向分解炉和换热管道加入的总给煤量的5％-50％。
  6. 根据权利要求5所述的水泥窑炉系统，其中：
    通过所述预热器给煤点加入的给煤量为所述给煤装置向分解炉和换热管道加入的总给煤量的20％-30％。
  7. 根据权利要求1所述的水泥窑炉系统，还包括：
    补燃风供给装置，用于向与设有预热器给煤点的换热管道相连的上级旋风筒的出口烟道提供补燃风。
  8. 根据权利要求1-7中任一项所述的水泥窑系统，还包括：
    水泥生料调温管道，其与设有预热器给煤点的相应换热管道相通。
  9. 根据权利要求8所述的水泥窑系统，其中：
    所述水泥生料调温管道设置有给料调节装置。
  10. 一种多级悬浮预热水泥窑炉系统的控制方法，所述水泥窑炉系统包括：回转窑，具有回转窑烟室；分解炉，与回转窑烟室连通；用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒与次末级旋风筒及两者之间的换热管道，其中：来自分解炉的烟气通入末级旋风筒，且在多级悬浮预热器的上下两级旋风筒之间，下级旋风筒的出口烟气通过换热管道连通到上级旋风筒，
    所述方法包括步骤：
    向至少一个换热管道供给煤粉，进入所述换热管道的煤粉在换热管道内被热解或者气化而形成煤焦和煤气。
  11. 根据权利要求10所述的方法，其中：
    向至少一个换热管道供给煤粉包括步骤：向位于末级旋风筒以及次末级旋风筒之间的换热管道供给煤粉。
  12. 根据权利要求10所述的方法，其中：
    向所述换热管道的给煤量为向分解炉和换热管道加入的总给煤量的5％-50％。
  13. 根据权利要求12所述的方法，其中：
    向所述换热管道的给煤量为向分解炉和换热管道加入的总给煤量的20％-30％。
  14. 根据权利要求10所述的方法，还包括步骤：
    向与给煤的换热管道相连的上级旋风筒的出口烟道提供补燃风。
  15. 根据权利要求10-14中任一项所述的方法，还包括步骤：
    向所述给煤的换热管道中通入水泥生料，以调节由于煤粉给入引起的温度变化。
  16. 一种多级悬浮预热水泥窑炉系统的控制方法，所述水泥窑炉系统 包括：回转窑，具有回转窑烟室；分解炉，与回转窑烟室连通；用于预热水泥生料的多级悬浮预热器，多级悬浮预热器至少包括末级旋风筒、次末级旋风筒及两者之间的换热管道，其中：来自分解炉的烟气通入末级旋风筒，且在多级悬浮预热器的上下两级旋风筒之间，下级旋风筒的出口烟气通过换热管道连通到上级旋风筒，
    所述方法包括步骤：
    向至少一个换热管道供给煤粉，使得与该换热管道对应的上级旋风筒内处于还原性气氛。
PCT/CN2020/077539 2019-03-12 2020-03-03 多级悬浮预热水泥窑炉系统及其控制方法 WO2020182012A1 (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201910186404.7A CN111689704B (zh) 2019-03-12 2019-03-12 多级悬浮预热水泥窑炉系统及其控制方法
CN201910186404.7 2019-03-12

Publications (1)

Publication Number Publication Date
WO2020182012A1 true WO2020182012A1 (zh) 2020-09-17

Family

ID=72426900

Family Applications (2)

Application Number Title Priority Date Filing Date
PCT/CN2020/077539 WO2020182012A1 (zh) 2019-03-12 2020-03-03 多级悬浮预热水泥窑炉系统及其控制方法
PCT/CN2020/077540 WO2020182013A1 (zh) 2019-03-12 2020-03-03 多级悬浮预热水泥窑炉系统及其控制方法

Family Applications After (1)

Application Number Title Priority Date Filing Date
PCT/CN2020/077540 WO2020182013A1 (zh) 2019-03-12 2020-03-03 多级悬浮预热水泥窑炉系统及其控制方法

Country Status (2)

Country Link
CN (1) CN111689704B (zh)
WO (2) WO2020182012A1 (zh)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113045224A (zh) * 2021-03-10 2021-06-29 中国中材国际工程股份有限公司 一种改造水泥熟料生产线制备粉状活性石灰的系统及方法
CN114199024A (zh) * 2021-11-23 2022-03-18 天瑞集团禹州水泥有限公司 一种水泥窑分解炉增加大还原区的脱硝系统
CN114777471A (zh) * 2022-05-07 2022-07-22 金华亨泰工程技术有限公司 一种节能、脱硝的水泥回转窑分解炉煤粉喷入方法
CN114788988A (zh) * 2022-05-16 2022-07-26 山东棱角建材科技有限公司 一种熟料生产线sncr精准脱硝工艺
CN114890645A (zh) * 2022-06-02 2022-08-12 天津中材工程研究中心有限公司 一种利用水泥窑高效资源化处置油泥的系统和方法

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112058064A (zh) * 2020-09-23 2020-12-11 南京凯盛国际工程有限公司 一种循环喷腾式NOx减排系统及其工作方法
CN112595096A (zh) * 2020-12-04 2021-04-02 贵州省鑫瀚蓝环保科技有限公司 一种水泥窑生产用脱氮燃烧方法
CN113149482A (zh) * 2021-05-25 2021-07-23 中国华能集团清洁能源技术研究院有限公司 一种在回转窑中处置废弃风机叶片的系统及其工作方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4123306A1 (de) * 1991-07-13 1993-01-21 Kloeckner Humboldt Deutz Ag Anlage zur thermischen behandlung von mehlfoermigen rohmaterialien
JP2000272940A (ja) * 1999-03-26 2000-10-03 Sumitomo Osaka Cement Co Ltd セメントクリンカー焼成工程における可燃性廃棄物の燃焼方法およびその装置
CN1418178A (zh) * 2000-03-30 2003-05-14 弗·尔·斯米德恩公司 利用颗粒状水泥原料生产水泥熟料的方法和设备
EP1334954A1 (de) * 2002-01-25 2003-08-13 KHD Humboldt Wedag AG Anlage zur Herstellung von Zementklinker
CN201281335Y (zh) * 2008-10-14 2009-07-29 南京凯盛水泥技术工程有限公司 一种用于水泥烧成的燃料分级燃烧装置
CN105444582A (zh) * 2015-12-16 2016-03-30 上海三橙能源科技有限公司 一种水泥窑旁路放风联合分级燃烧窑尾烟气处理装置及工艺方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS56166922A (en) * 1980-05-27 1981-12-22 Kawasaki Heavy Ind Ltd Reduction of nitrogen oxide in waste gas from cement kiln
CN102923979B (zh) * 2012-10-19 2014-07-23 安徽海螺建材设计研究院 干法水泥窑熟料生产线及其脱硝工艺方法
CN105805739B (zh) * 2014-08-29 2019-07-23 中国科学院工程热物理研究所 调节过热蒸汽温度的循环流化床燃烧方法
CN104566349A (zh) * 2015-01-20 2015-04-29 安徽海螺建材设计研究院 采用脱氮技术的新型干法水泥窑空气分级燃烧系统
CN106066126A (zh) * 2016-07-27 2016-11-02 北京凯盛建材工程有限公司 一种应用于水泥窑炉降低水泥窑NOx排放量的全过程低氮燃烧技术
CN108261843A (zh) * 2017-12-22 2018-07-10 成都京龙科技有限公司 高效快速降低回转窑氮氧化合物的装置及方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4123306A1 (de) * 1991-07-13 1993-01-21 Kloeckner Humboldt Deutz Ag Anlage zur thermischen behandlung von mehlfoermigen rohmaterialien
JP2000272940A (ja) * 1999-03-26 2000-10-03 Sumitomo Osaka Cement Co Ltd セメントクリンカー焼成工程における可燃性廃棄物の燃焼方法およびその装置
CN1418178A (zh) * 2000-03-30 2003-05-14 弗·尔·斯米德恩公司 利用颗粒状水泥原料生产水泥熟料的方法和设备
EP1334954A1 (de) * 2002-01-25 2003-08-13 KHD Humboldt Wedag AG Anlage zur Herstellung von Zementklinker
CN201281335Y (zh) * 2008-10-14 2009-07-29 南京凯盛水泥技术工程有限公司 一种用于水泥烧成的燃料分级燃烧装置
CN105444582A (zh) * 2015-12-16 2016-03-30 上海三橙能源科技有限公司 一种水泥窑旁路放风联合分级燃烧窑尾烟气处理装置及工艺方法

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113045224A (zh) * 2021-03-10 2021-06-29 中国中材国际工程股份有限公司 一种改造水泥熟料生产线制备粉状活性石灰的系统及方法
CN114199024A (zh) * 2021-11-23 2022-03-18 天瑞集团禹州水泥有限公司 一种水泥窑分解炉增加大还原区的脱硝系统
CN114777471A (zh) * 2022-05-07 2022-07-22 金华亨泰工程技术有限公司 一种节能、脱硝的水泥回转窑分解炉煤粉喷入方法
CN114777471B (zh) * 2022-05-07 2023-09-01 金华亨泰工程技术有限公司 一种节能、脱硝的水泥回转窑分解炉煤粉喷入方法
CN114788988A (zh) * 2022-05-16 2022-07-26 山东棱角建材科技有限公司 一种熟料生产线sncr精准脱硝工艺
CN114890645A (zh) * 2022-06-02 2022-08-12 天津中材工程研究中心有限公司 一种利用水泥窑高效资源化处置油泥的系统和方法
CN114890645B (zh) * 2022-06-02 2023-09-01 天津中材工程研究中心有限公司 一种利用水泥窑高效资源化处置油泥的系统和方法

Also Published As

Publication number Publication date
CN111689704A (zh) 2020-09-22
CN111689704B (zh) 2021-10-08
WO2020182013A1 (zh) 2020-09-17

Similar Documents

Publication Publication Date Title
WO2020182012A1 (zh) 多级悬浮预热水泥窑炉系统及其控制方法
CN101608866B (zh) 能够处理带可燃物生料的水泥窑外预分解窑尾系统
CN101269919B (zh) 一种煅烧物料的竖窑装置
CN104058606B (zh) 富氧燃烧生产石灰的方法和装置
US5816795A (en) Apparatus and method for providing supplemental fuel to a preheater/precalciner kiln
CN109574523B (zh) 一种气化炉高温煤气热送直接燃烧的石灰窑
CN101475324A (zh) 电石渣干烧制水泥熟料的工艺方法
CN107084617B (zh) 一种水泥旋风预热器窑改造为窑外预分解窑的节能减排改造方法
CN101322001A (zh) 用于制造水泥熟料的设备以及用于运行这种设备的方法
US20200392041A1 (en) Clinker production plant and method for producing clinker in such a plant
CN103175398B (zh) 一种燃重油新型干法水泥生产的预分解系统
CN201297860Y (zh) 一种电石渣全部替代石灰石煅烧水泥的装置
CN113465366A (zh) 一种回转窑低氮燃烧装置及生产方法
CN211445544U (zh) 一种水泥窑运用外燃式回转窑捕集纯化co2和减排系统
CN201497351U (zh) 水泥窑外预分解窑尾系统
CN203947032U (zh) 富氧燃烧生产石灰的装置
CN112844003B (zh) 多级悬浮预热器及控制方法、水泥熟料生成设备控制方法
CN113072310B (zh) 一种石灰窑及石灰制备方法
CN105605584B (zh) 一种在水泥窑中利用富氧处置固废的方法
CN114956610A (zh) 一种电石渣悬浮煅烧系统
CN209685619U (zh) 一种气化炉高温煤气热送直接燃烧的石灰窑
CN210625308U (zh) 独立煤粉输送系统和应用其的水泥窑炉
CN101195521B (zh) 一种在水泥回转窑预分解炉利用钢铁生产中富余煤气的方法
CN111960698A (zh) 工业窑炉设备的燃料供给系统及方法、工业窑炉设备
CN215810193U (zh) 一种用于水泥窑的管式增产脱硝一体化装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20769919

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 20769919

Country of ref document: EP

Kind code of ref document: A1