WO2020164259A1 - 具有高效烟气脱硫的回转石灰窑预热器 - Google Patents

具有高效烟气脱硫的回转石灰窑预热器 Download PDF

Info

Publication number
WO2020164259A1
WO2020164259A1 PCT/CN2019/115227 CN2019115227W WO2020164259A1 WO 2020164259 A1 WO2020164259 A1 WO 2020164259A1 CN 2019115227 W CN2019115227 W CN 2019115227W WO 2020164259 A1 WO2020164259 A1 WO 2020164259A1
Authority
WO
WIPO (PCT)
Prior art keywords
flue gas
preheater
sulfur
lime kiln
rotary lime
Prior art date
Application number
PCT/CN2019/115227
Other languages
English (en)
French (fr)
Inventor
庞焕军
张林进
王云龙
沈浩
赵波
Original Assignee
江苏中圣园科技股份有限公司
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 江苏中圣园科技股份有限公司 filed Critical 江苏中圣园科技股份有限公司
Publication of WO2020164259A1 publication Critical patent/WO2020164259A1/zh

Links

Images

Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/81—Solid phase processes
    • B01D53/83—Solid phase processes with moving reactants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/25—Process efficiency

Definitions

  • the invention relates to a lime kiln flue gas desulfurization equipment, in particular to a rotary lime kiln preheater with efficient flue gas desulfurization.
  • flue gas desulfurization technologies mainly include dry, semi-dry and wet desulfurization. These technical solutions generally use calcium-based desulfurizers.
  • the calcium-based desulfurizer and the SO 2 in the flue gas generate CaSO 3 , which is further oxidized to CaSO 4 at high temperature. So that SO 2 gas is removed from the flue gas and fixed in the desulfurizing agent.
  • the input material is limestone based on calcium carbonate
  • the product is lime based on calcium oxide. Both have the ability to absorb SO 2 and are commonly used calcium-based desulfurizers.
  • mainstream rotary lime kilns are equipped with vertical preheaters to recover the waste heat of high-temperature flue gas emitted during the limestone calcination process.
  • the limestone material is first stored in the top silo of the lime kiln preheater, and enters the annular heating space in the middle of the vertical preheater through the discharge pipe. In the annular heating space, the limestone material moves from top to bottom, the high temperature flue gas flows from bottom to top, and the limestone material and the high temperature flue gas conduct heat and mass transfer while countercurrently flowing. During the falling process of the limestone material, the limestone particles are gradually heated and decomposed by the high-temperature flue gas. The outer surface of the limestone is first decomposed into calcium oxide.
  • the limestone particles are heated to about 900-1100°C. 30% of limestone is decomposed; while the flue gas is rising, the heat of the high-temperature flue gas is transferred to the limestone material, and the temperature of the flue gas itself gradually decreases during the rising process.
  • the flue gas temperature drops To about 260 ⁇ 300°C.
  • the limestone falling near the cone at the bottom of the preheater is pushed into the feeding chute by the push rod device, and then enters the rotary kiln for calcination.
  • the material and the material will collide on the outer surface, and the calcium oxide layer formed on the outermost layer of the material will be broken into calcium oxide powder.
  • the limestone material when the limestone material is calcined in the rotary kiln, the limestone material continuously rolls and rubs against the kiln wall.
  • the calcium oxide layer generated on the outside of the limestone material will also fall off and break due to the collision and friction with the kiln wall, resulting in a large amount of small particle size Of calcium oxide powder.
  • the calcium oxide powder is dispersed in the flue gas, moves with the flow of the flue gas, and part of it enters the fired product; part of it enters the exhaust pipe and is captured by the dust removal equipment.
  • the Ca/S ratio in the kiln far meets the ratio required for desulfurization, but the desulfurization rate is still low, and SO in the flue gas 2 is too high to meet environmental protection requirements, and additional flue gas desulfurization equipment needs to be added.
  • the reaction between calcium oxide and SO 2 to form calcium sulfite is a reversible reaction.
  • the calcium sulfite produced will be quickly oxidized to calcium sulfate, which has high temperature stability.
  • the sulfur fixation reaction is a reversible process, and temperature has an important influence on the reaction process.
  • the temperature is low, the reaction speed is slow, and the reaction rate is too high, the reaction rate is fast, but the decomposition of the sulfur product will occur, and the reaction will proceed in the direction of precipitation of SO 2 , especially when the temperature is higher than 1200°C A large amount of SO 2 is precipitated.
  • the present invention modifies the rotary lime kiln, and aims to provide a rotary lime kiln preheater with efficient flue gas desulfurization.
  • the present invention provides a rotary lime kiln preheater with efficient flue gas desulfurization, which includes a preheater main body, a top silo, a discharge pipe, a smoke exhaust pipe, a push rod device, and a discharge chute. It also includes a sulfur-fixing agent auxiliary agent delivery pipeline, and the lower end of the sulfur-fixing agent auxiliary agent delivery pipeline is provided with a nozzle, and the nozzle is located above the discharging chute.
  • the powder of the sulfur-fixing agent auxiliary agent can be transported to the upper part of the blanking chute in the main body of the preheater through the sulfur-fixing agent auxiliary delivery pipeline under the action of high-speed air flow.
  • the nozzle is sprayed through the nozzle to mix with the high-temperature flue gas from the rotary lime kiln to improve the microstructure of the sulfur-fixing agent (ie calcium oxide in the rotary lime kiln) and delay the high-temperature decomposition of the desulfurization product (ie calcium sulfite) , Increase its decomposition temperature.
  • the sulfide-fixing agent auxiliary agent delivery pipeline is arranged at the center of the main body of the preheater.
  • the sulfur-fixing agent auxiliary agent and the high-temperature flue gas flow can be mixed uniformly.
  • the main body of the preheater includes an inner plate and an outer plate that collectively enclose an annular heating space.
  • the annular heating space includes a low temperature section, a desulfurization section, and a high temperature section.
  • the desulfurization section is set such that the cross section from top to bottom increases first and then changes. Small to increase the residence time of the material in the desulfurization section.
  • the residence time of the material in the temperature range of 800-900°C in the preheater can be increased.
  • the inner plate of the desulfurization section has a first inclined part and a second inclined part.
  • the first inclined part is set so that its horizontal inclination angle is smaller than the accumulation angle of the material
  • the second inclined part is set so that the horizontal inclination angle is greater than the The friction angle between the plates.
  • the arrangement of the first inclined portion and the second inclined portion can fill the entire annular heating space without affecting the movement of the stone material.
  • the inner plate is further provided with a vertical portion between the first inclined portion and the second inclined portion.
  • the temperature of the aforementioned desulfurization section is set to 800-900°C.
  • the above-mentioned rotary lime kiln preheater with high-efficiency flue gas desulfurization further includes a flue gas swirling flow diversion water spray device, and the flue gas swirl flow diversion water spraying device is installed at the inlet end of the smoke exhaust pipe.
  • the above-mentioned smoke swirling flow guiding water spray device includes an upper fixing ring, a lower fixing plate, a nozzle installed on the lower solid top plate and facing the inside of the smoke swirling flow guiding water spray device, a water pipe connected to the nozzle, A plurality of baffles are fixed between the upper fixing ring and the lower fixing plate, and the plurality of baffles are tangentially distributed around an internal imaginary circle of the flue gas swirl flow guiding water spray device.
  • the flow direction of the flue gas into the exhaust pipe can be changed by the arrangement of the deflector, so that the direction of the flue gas flowing into the exhaust pipe is changed from along the axial direction of the exhaust pipe to along the exhaust pipe. Tangentially, this can 1) increase the contact time between calcium oxide and flue gas, and 2) accelerate the heat and mass transfer between water droplets and flue gas.
  • the plurality of baffles are uniformly distributed along the tangential direction of the inner imaginary circle.
  • the radius of the aforementioned inner imaginary circle is half of the radius of the smoke exhaust pipe.
  • This setting enables the flue gas to form a strong swirling flow in the flue gas swirling diversion water spray device.
  • Figure 1 is a schematic diagram of the internal structure of a rotary lime kiln preheater with efficient flue gas desulfurization according to an embodiment of the present invention
  • FIG 2 is a schematic diagram of the annular heating space of the rotary lime kiln preheater with high-efficiency flue gas desulfurization shown in Figure 1. This figure clearly shows that the desulfurization section of the annular heating space becomes larger and then smaller from top to bottom structure;
  • Figure 3 is the flue gas swirling diversion water spray device of the rotary lime kiln preheater with high efficiency flue gas desulfurization shown in Figure 1.
  • a rotary lime kiln preheater with high-efficiency flue gas desulfurization includes a top silo 1, a preheater main body 2, a discharge pipe 3, a smoke exhaust pipe 4, a pusher
  • the rod device 5 and the discharging chute 6 further include a sulfur-fixing agent auxiliary agent delivery pipeline 7.
  • the lower end of the sulfur-fixing agent auxiliary agent delivery pipeline 7 is provided with a nozzle 70, and the nozzle 70 is located above the feeding chute 6.
  • the sulfur-fixing agent auxiliary agent delivery pipeline 7 is arranged at the center of the preheater main body 2.
  • the preheater main body 2 includes an inner plate 21 and an outer plate 22 that collectively enclose an annular heating space 20.
  • the annular heating space 20 includes a low-temperature section, a desulfurization section and a high-temperature section.
  • the desulfurization section is set to increase and then decrease the cross section from top to bottom (see Figure 2) to increase the residence time of the material in the desulfurization section.
  • the inner plate 21 has a first inclined portion 210, a vertical portion 211, and a second inclined portion 212.
  • the first inclined portion 210 is set such that its horizontal inclination angle ⁇ is smaller than the accumulation angle of the material
  • the second inclined portion 212 is set such that its horizontal inclination angle ⁇ is greater than the friction angle between the material and the inner plate, as shown in FIG. 3.
  • the rotary lime kiln preheater further includes a flue gas swirling flow diversion water spray device 8 installed in The inlet end of the exhaust pipe 4.
  • the flue gas swirling flow guiding water spray device 8 includes an upper fixing ring 81, a lower fixing plate 83, and a device installed on the lower solid top plate 83 and facing the inside of the flue gas swirling flow guiding water spray device 8.
  • the nozzle 85, a water pipe 87 connected to the nozzle 85, and a plurality of baffle plates 82 fixed between the upper fixing ring 81 and the lower fixing plate 83.
  • the plurality of baffles 82 are evenly distributed tangentially around an internal imaginary circle (not shown) of the flue gas swirl flow diversion water spray device.
  • the radius of the internal imaginary circle is half of the radius of the smoke exhaust pipe 4.
  • the measures taken in this embodiment are as follows: 1) Inject the sulfur-fixing agent auxiliary agent through the sulfur-fixing agent auxiliary agent delivery pipe 7 into the upper part of the chute 6 , Some sulfur-fixing agent additives can improve the microstructure of the sulfur-fixing agent (ie calcium oxide), and other sulfur-fixing agent additives can delay the high temperature decomposition of the desulfurization product (ie calcium sulfite) and increase its decomposition temperature; 2) The inlet end of the exhaust pipe 4 is additionally provided with a flue gas swirling flow diversion water spray device 8 to reactivate the calcium oxide, increase the reaction speed of the low temperature section in the annular heating space 20, and increase the sulfur fixation rate; 3) change the preheater body 2 The structure of the annular heating space 20 increases the volume of the optimum temperature zone and increases the residence time of the material in this temperature zone.
  • the ground sulfur-fixing agent powder is transported to the nozzle 70 above the high-temperature section of the blanking chute 6 in the annular heating space 20 through the sulfur-fixing agent delivery pipeline 7 under the action of high-speed airflow, and the sulfur-fixing agent is carried.
  • the air flow of the additive powder is uniformly mixed with the high temperature flue gas flow from the rotary kiln.
  • the additives for improving the microstructure of the sulfur-fixing agent generally include alkali metal compounds and organic solutions.
  • the addition of these additives can improve the micropore diameter, internal structure of the pores, pore specific surface area, and pore distribution of the sulfur-fixing agent. Thereby improving the activity of the sulfur-fixing agent, thereby increasing the sulfur-fixing rate.
  • the alkali metal compound additives mainly include Na 2 CO 3 , NaCl, and KCl.
  • the addition of Na 2 CO 3 can promote the rearrangement of the CaO lattice, improve the pore distribution and pore size, and inhibit the high temperature decomposition of sulfur fixation products.
  • the presence of NaCl and KCl improves the efficiency of CaO in the process of sulfur fixation.
  • Sulfur-fixing agent additives are added to the sulfur-fixing agent to form sulfur-containing minerals with high temperature thermal stability or to form a low-temperature eutectic as an additive to prevent the decomposition of CaSO 4 .
  • These sulfur fixative additives mainly include:
  • the addition of iron and silicon components can generate a Ca-Fe-Si-O system to form a heat-resistant silicate stable phase.
  • Calcium sulfate is covered or wrapped by high melting point silicate, effectively preventing the re-decomposition of calcium sulfate , Can significantly improve the desulfurization rate at high temperature;
  • Fe 2 O 3 accelerates the reaction rate of calcium oxide and sulfur dioxide, and calcium sulfite is easily oxidized to calcium sulfate at high temperature;
  • Al 2 O 3 can also inhibit the high-temperature decomposition of sulfur fixation products, and at the same time can form a double salt of CaSO 4 ⁇ CaO ⁇ Al 2 O 3 with high thermal stability, and this product can cover or wrap the surface of Ca S O 4 crystals. Inhibit its decomposition and effectively improve the sulfur fixation effect;
  • MgO promotes the sulfur fixation reaction of CaO and can catalyze the sulfur fixation reaction of lime
  • the main components of the sulfur-fixing agent auxiliary are Al 2 O 3 , SiO 2 , MgO, Fe 2 O 3 , and a small amount of alkali metal compounds are used as auxiliary components.
  • the amount of sulfur-fixing agent sprayed is based on the sulfur content in the flue gas, and the Ca/S ratio is 2, and the total amount of CaO required to absorb the sulfur in the flue gas is back calculated.
  • the amount of the auxiliary agent is 2 ⁇ 6% of total CaO required.
  • the flue gas makes a high-speed swirling motion in the exhaust pipe 4, the flue gas and water mix more evenly, accelerate the heat and mass transfer of water droplets and flue gas, and promote calcium oxide in the flue gas , The reaction of water droplets and sulfur dioxide to prevent the lime powder in the flue gas from agglomerating and blocking the exhaust pipe 4 due to water absorption;
  • the most suitable temperature range for sulfur fixation reaction is 800 ⁇ 900°C. If the temperature exceeds 900°C, part of the sulfur fixation products will decompose and reduce the overall sulfur fixation rate; if the temperature is below 800°C, the reaction rate will decrease, which is not conducive to the rapid progress of the sulfur fixation reaction.
  • the structure of the traditional preheater is similar to the circular cross-section enclosed by the inner and outer dodecagons and is formed by stretching to a certain height.
  • the flue gas flows in this space with a constant cross-section, which has the greatest impact on the entire desulfurization reaction in the 800-900 °C area It only occupies a small part of the entire material layer.
  • the flue gas flows through this area at high speed, with short residence time and low desulfurization rate.
  • the present invention designs a new type of preheater structure, namely: in the limestone material at 800-900°C, the preheater body structure is changed from a uniform cross-section ring structure to a variable cross-section ring structure.
  • the horizontal section of this area is First it becomes bigger, then smaller, and finally returns to the original size.
  • the purpose is to increase the residence time of the stone in the 800-900°C area.
  • the cross section first consider the influence of the accumulation angle of the stone.
  • the horizontal inclination angle ⁇ of the first inclined part 210 should be slightly smaller than the accumulation angle of the stone; secondly, in order not to affect the falling of the stone, the influence of the friction angle of the stone should be considered.
  • the horizontal inclination angle ⁇ of the second inclined portion 212 should be slightly larger than the friction angle of the stone.
  • the height of the material surface can be adjusted by increasing the height of the preheater, that is, increasing the height of the annular heating space 20.
  • the preheating can be controlled by changing the input and output volume (for example, by adjusting the movement frequency of the push rod device 5) The total height of the material layer in the annular heating space 20 inside the device.
  • Increasing the feed volume and reducing the discharge volume will increase the total height of the material layer, resulting in an increase in the resistance of the material layer, and a decrease in the flue gas flow velocity, thereby extending the residence time of the flue gas in the desulfurization section of the annular heating space 20; Conversely, reducing the amount of feed and increasing the amount of output will reduce the total height of the material layer, reduce the gap resistance of the material layer, and increase the flue gas flow rate, thereby shortening the residence time of the flue gas in the desulfurization section of the preheater.
  • the flue gas swirling diversion water spray device 8 is installed at the entrance of the flue gas pipe 4, where the flue gas temperature is about 260 ⁇ 300 °C, the water droplets can absorb the heat of the flue gas and evaporate, and the lime powder will not change due to water absorption Reunite into a paste. Moreover, because the flue gas temperature is not high, the water droplets can stay for enough time to activate the desulfurization reaction;
  • the flue gas swirling diversion water spray device 8 changes the way the flue gas enters the exhaust pipe 4, from the original axial entry to the tangential entry, the mixture of flue gas, water droplets, and lime powder is more uniform and strong, and the water droplets and smoke
  • the heat and mass transfer resistance of gas is smaller, and the flue gas desulfurization effect is better at low temperature;
  • sulfur-fixing agent additives in the high-temperature section of the annular heating space 20 improves the micro-pore structure of the sulfur-fixing agent, which is conducive to the sulfur-fixing reaction.
  • the surface of the sulfur-fixing product is covered with a substance with high temperature stability to reduce the re-sulfurization Decompose, increase the decomposition temperature of sulfur fixation products;
  • variable cross-section structure design of the desulfurization section of the annular heating space 20 of the preheater takes into account the accumulation angle of the stone and the friction angle between the stone and the inner plate, and the stone can better fill the entire ring of the preheater during the falling process Heating space 20;
  • the design and manufacture of the preheater take into account the surplus of the material layer height. In actual production, the balance between the inlet and the output of the preheater is adjusted according to the needs, and then the height of the material layer inside the preheater is adjusted.

Landscapes

  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

本发明涉及一种具有高效烟气脱硫的回转石灰窑预热器，其包括预热器主体、顶部料仓、下料管、排烟管、推杆装置、下料溜槽，还包括固硫剂助剂输送管道，该固硫剂助剂输送管道的下端设置有喷嘴，该喷嘴位于下料溜槽的上方。本发明通过固硫剂助剂输送管道的设置，固硫剂助剂粉末能够在高速气流的作用下通过该固硫剂助剂输送管道输送至预热器主体内下料溜槽上方的喷嘴，并经由喷嘴喷出以与来自回转石灰窑的高温烟气流混合，来改善固硫剂微观结构、延缓脱硫产物的高温分解，提高其分解温度。

Description

具有高效烟气脱硫的回转石灰窑预热器 技术领域：
本发明涉及一种石灰窑烟气脱硫设备，特别涉及一种具有高效烟气脱硫的回转石灰窑预热器。
背景技术：
目前烟气脱硫技术主要有干法、半干法以及湿法脱硫，这些技术方案普遍采用钙基脱硫剂。钙基脱硫剂与烟气中的SO 2生成CaSO 3，高温下进一步氧化成CaSO 4。从而使SO 2气体从烟气中脱除、被固定在脱硫剂中。
对于石灰窑来说，投入的原料是以碳酸钙为主的石灰石，产品是以氧化钙为主的石灰，两者都具有吸收SO 2的能力，都是常用的钙基脱硫剂。
目前主流的回转石灰窑都配备有竖式预热器,以能够回收石灰石煅烧过程中排放的高温烟气的余热。石灰石料首先被储存在石灰窑预热器顶部料仓，经下料管进入竖式预热器中部的环形加热空间内。在环形加热空间内，石灰石料自上而下运动，高温烟气自下而上流动，石灰石料与高温烟气逆流的同时进行传热传质。石灰石料下落过程中，石灰石颗粒逐渐被高温烟气加热而分解，其外表面最先分解成氧化钙，到达预热器底部锥斗附近时，石灰石颗粒被加热到900～1100℃左右，大概有30％的石灰石分解；烟气在上升过程中，高温烟气的热量传递到石灰石料，烟气自身温度在上升过程中逐步下降，到达预热器上部的排烟管附近时，烟气温度降到260～300℃左右。下落到预热器底部锥斗附近的石灰石料被推杆装置推入下料溜槽，进入回转窑内煅烧。
石灰石料在预热下降过程中，物料与物料之间在外表面会发生碰撞，物料最外层生成的氧化钙层会因此而破碎成氧化钙粉末。同时石灰石料在回转窑内煅烧时，石灰石料不断地翻滚运动、摩擦窑壁，石灰石料外侧生成的氧化钙层也会因与窑壁的碰撞、摩擦而脱落、破碎，产生大量的粒径微小的氧化钙粉末。在高速烟气的冲击下，氧化钙粉末分散于烟气中，随烟气的流动 而运动，部分进入烧成产品中；部分进入排烟管，被除尘设备捕集下来。
虽然石灰窑内有大量的石灰，同时大量粒径微小的氧化钙粉末分布于烟气中，窑内Ca/S比值远远满足脱硫所需的比值，但脱硫率依然较低，排烟中SO 2偏高，不能满足环保的要求，还需要再添加额外的烟气脱硫设备。
而且，氧化钙与SO 2生成亚硫酸钙的反应是个可逆反应，温度越高反应速率越大，但当温度高到一定温度后，亚硫酸钙分解速度将大于其生成速度。在高温下，在有O 2存在时，生成的亚硫酸钙将快速被氧化为硫酸钙，硫酸钙具有高温稳定性。
总之，造成氧化钙脱硫率低有如下因素：
1)与氧化钙微观结构有关：石灰石料反应进行一段时间后，氧化钙颗粒表面孔隙很快被堵塞，从而阻止了SO 2向其内部的扩散，使固硫率下降；
2)氧化钙与SO 2是个气固反应，随着反应的进行，氧化钙活性降低；
3)固硫反应是可逆过程，温度对反应进程有着重要的影响。温度低，反应速度慢，向着生成固硫产物的方向进行；温度太高，反应速率快，但是会发生固硫产物分解，反应向着析出SO 2的方向进行，尤其温度高于1200℃时会有大量的SO 2析出。
发明内容：
为克服上述问题，针对回转石灰窑自身的热工特性，本发明对回转石灰窑进行改造，旨在提供一种具有高效烟气脱硫的回转石灰窑预热器。
为实现上述目的，本发明提供一种具有高效烟气脱硫的回转石灰窑预热器，其包括预热器主体、顶部料仓、下料管、排烟管、推杆装置、下料溜槽，还包括固硫剂助剂输送管道，该固硫剂助剂输送管道的下端设置有喷嘴，该喷嘴位于下料溜槽的上方。
在本发明中，通过固硫剂助剂输送管道的设置，固硫剂助剂粉末能够在高速气流的作用下通过该固硫剂助剂输送管道输送至预热器主体内下料溜槽上方的喷嘴，并经由喷嘴喷出以与来自回转石灰窑的高温烟气流混合，来改 善固硫剂(即回转石灰窑内的氧化钙)微观结构、延缓脱硫产物(即亚硫酸钙)的高温分解，提高其分解温度。
进一步，固硫剂助剂输送管道布置在预热器主体的中心位置。
通过上述设置，能够使固硫剂助剂与高温烟气流混合均匀。
进一步，上述预热器主体包括共同围成环形加热空间的内板和外板，该环形加热空间包括低温段、脱硫段和高温段，该脱硫段设置成由上到下截面先变大再变小以增加物料在该脱硫段内的驻留时间。
通过上述结构设置，能够增加物料在预热器内800～900℃温度区间内的停留时间。
再进一步，在上述脱硫段内板具有第一倾斜部和第二倾斜部，第一倾斜部设置成其水平倾斜角小于物料的堆积角，第二倾斜部设置成其水平倾斜角大于物料与内板间的摩擦角。
通过第一倾斜部和第二倾斜部的设置，能够不影响石料的运动并充满整个环形加热空间。
又进一步，上述内板在第一倾斜部和第二倾斜部之间还设置有竖直部。
还进一步，上述脱硫段的温度设置为800～900℃。
还进一步，上述具有高效烟气脱硫的回转石灰窑预热器还包括烟气旋流导流喷水装置，该烟气旋流导流喷水装置装设于排烟管的入口端。
在排烟管入口端增设烟气旋流导流喷水装置，再次活化氧化钙，增加预热器主体内低温区域的反应速度，提升固硫率；
再进一步，上述烟气旋流导流喷水装置包括上固定环、下固定板、装设于下固顶板上并朝向烟气旋流导流喷水装置内部的喷嘴、与喷嘴连接的水管、固定于上固定环和下固定板之间的多个导流板，该多个导流板围绕烟气旋流导流喷水装置的一个内部假想圆切向分布。
通过上述结构设置，能够借助于导流板的排布来改变烟气进入排烟管内的流动方向，使得烟气流入排烟管的方向由沿着排烟管轴向变为沿着排烟管切向，这样能够1)增加氧化钙与烟气的接触时间、2)加快水滴与烟气的传 热传质。
又进一步，上述多个导流板沿着内部假想圆切向均匀分布。
还进一步，上述内部假想圆的半径为排烟管的半径的一半。
这一设置使得烟气能够在烟气旋流导流喷水装置内形成强烈的旋流流动。
通过参考下面所描述的实施例，本发明的上述这些方面和其他方面将会得到更清晰地阐述。
附图说明：
发明的结构以及进一步的目的和优点将通过下面结合附图的描述得到更好地理解，其中，相同的参考标记标识相同的元件：
图1是根据本发明的一个具体实施方式的具有高效烟气脱硫的回转石灰窑预热器的内部结构示意图；
图2是图1所示具有高效烟气脱硫的回转石灰窑预热器的环形加热空间示意图，该图清楚地示出了环形加热空间的脱硫段由上到下截面先变大再变小的结构；
图3是图1所示具有高效烟气脱硫的回转石灰窑预热器的烟气旋流导流喷水装置。
具体实施方式：
下面将结合附图描述本发明的具体实施方式。
如图1所示，根据本发明的一个具体实施方式的具有高效烟气脱硫的回转石灰窑预热器包括顶部料仓1、预热器主体2、下料管3、排烟管4、推杆装置5、下料溜槽6，还包括固硫剂助剂输送管道7，该固硫剂助剂输送管道7的下端设置有喷嘴70，该喷嘴70位于下料溜槽6的上方。优选地，固硫剂助剂输送管道7布置在预热器主体2的中心位置。
如图1所示，并参考图2和图3，预热器主体2包括共同围成环形加热空 间20的内板21和外板22。该环形加热空间20包括低温段、脱硫段和高温段，该脱硫段设置成由上到下截面先变大再变小(见图2)，以增加物料在该脱硫段内的驻留时间。在脱硫段(温度为800～900℃)，内板21具有第一倾斜部210、竖直部211、第二倾斜部212，第一倾斜部210设置成其水平倾斜角α小于物料的堆积角，第二倾斜部212设置成其水平倾斜角β大于物料与内板间的摩擦角，如图3所示。
如图1所示，并参考图3，在本实施方式中，回转石灰窑预热器还包括烟气旋流导流喷水装置8，该烟气旋流导流喷水装置8装设于排烟管4的入口端。如图3所示，该烟气旋流导流喷水装置8包括上固定环81、下固定板83、装设于下固顶板83上并朝向烟气旋流导流喷水装置8内部的喷嘴85、与喷嘴85连接的水管87、固定于上固定环81和下固定板83之间的多个导流板82。该多个导流板82围绕烟气旋流导流喷水装置的一个内部假想圆(图未示)切向均匀分布。在本实施方式中，该内部假想圆的半径为排烟管4的半径的一半，当然，这只是其中一个实例，也可以设置成该“一半”左右的其它数值，只要能够使烟气在烟气旋流导流喷水装置8内形成强烈的旋流流动就可以，太小或太大对旋流流动都不利。
总的来说，针对现有技术中氧化钙脱硫率低的现象，本实施方式采取的措施有：1)将固硫剂助剂通过固硫剂助剂输送管道7喷入下料溜槽6上方，一些固硫剂助剂能够改善固硫剂(即氧化钙)的微观结构，另一些固硫剂助剂能够延缓脱硫产物(即亚硫酸钙)的高温分解，提高其分解温度；2)在排烟管4的入口端增设烟气旋流导流喷水装置8，再次活化氧化钙，增加环形加热空间20中低温段的反应速度，提升固硫率；3)改变预热器主体2中环形加热空间20的结构，增加最适温度区的容积，增加物料在此温度区域内的停留时间。
针对上述措施1)～3)，其具体操作措施介绍如下：
1)将磨制好的固硫剂助剂粉末，在高速气流的作用下通过固硫剂助剂输送管道7输送至环形加热空间20高温段下料溜槽6的上方的喷嘴70，携带固硫剂助剂粉末的气流与来自回转窑的高温烟气流均匀混合。
需要说明的是，改善固硫剂微观结构的助剂一般有碱金属化合物和有机溶液，这些助剂的添加能够改善固硫剂微孔直径大小、孔内部结构、孔比表面积、孔分布等，从而提高固硫剂的活性，进而提高固硫率。其中碱金属化合物助剂主要有Na 2CO 3、NaCl、KCl。Na 2CO 3的加入可以促进CaO晶格重排，改善孔的分布和孔的尺寸，抑制固硫产物的高温分解。NaCl、KCl的存在提高了CaO在固硫过程中的效率，这是因为在反应过程中会形成一薄层的NaCl/CaO,KCl/CaO低共熔层，增加钠、钾离子的迁移和扩散能力，导致CaO晶格结构的改变，从而改善CaO性质。
固硫剂助剂添加到固硫剂中，能够形成具有高温热稳定性含硫矿物或形成低温共熔物包裹并阻止CaSO 4分解的添加剂。这些固硫剂助剂主要有：
铁、硅组分的添加，能够生成Ca-Fe-Si-O体系，形成一种耐热硅酸盐稳定相，硫酸钙被高熔点硅酸盐覆盖或包裹，有效阻止了硫酸钙的再分解，能够明显提高高温下的脱硫率；
Fe 2O 3加快氧化钙与二氧化硫的反应速率，亚硫酸钙高温下易氧化成硫酸钙；
Al 2O 3也可以抑制固硫产物的高温分解，同时可以形成具有高热稳定性的CaSO 4·CaO·Al 2O 3的复盐，且此产物可以覆盖或包裹Ca SO 4晶体的表面，抑制其分解，有效提高固硫效果；
MgO对CaO的固硫反应起促进作用，能够催化石灰固硫反应；
因此，固硫剂助剂主要成分为Al 2O 3、SiO 2、MgO、Fe 2O 3，微量的碱金属化合物做为辅助成分。
喷入的固硫剂助剂的量是根据烟气中的的含硫量，按照Ca/S比为2，反算出吸收烟气中的硫需要的总CaO量，助剂的量按2～6％所需总CaO量计。
2)在回转石灰窑预热器的环形加热空间20内排烟管4的入口端增设烟气旋流导流喷水装置8，这能够使得：
⑴活化石灰脱硫反应，增加反应速度；
⑵改变烟气进入排烟管4内的流动方向：烟气流入排烟管4的方向由沿 着排烟管4轴向变为沿着排烟管4切向，带来的好处：
A)颗粒物竖直方向的速度降低，由于颗粒受重力的影响，相应地烟气中裹挟的部分颗粒会在重力的作用下落入预热器上部空间，增加了氧化钙与烟气接触时间；
B)在导流板82的作用下，烟气在排烟管4内做高速旋流运动，烟气与水混合更加均匀，加快水滴与烟气的传热传质，促进烟气中氧化钙、水滴和二氧化硫的反应，避免烟气中的石灰粉因吸水而团聚堵塞排烟管4；
C)喷入的水滴在排烟管4负压作用下，全部经排烟管4路被吸入到管道内，避免喷入的水滴影响石灰石料的预热。
3)改变预热器本体结构
固硫反应最适宜温度区间为800～900℃。温度超过900℃，部分固硫产物会发生分解，降低总体固硫率；温度低于800℃，反应速率降低，不利于固硫反应的快速进行。
传统的预热器结构类似于由内、外十二边形围成的环形截面拉伸一定高度形成，烟气在此空间内做等截面流动，对整个脱硫反应影响最大的800～900℃区域只占整个料层很小的一部分，烟气流高速通过此区域，停留时间短，脱硫率低。
针对此问题，本发明设计一种新型预热器结构，即：在石灰石料800～900℃区域，将预热器本体结构由等截面的环形结构为变截面的环形结构，此区域的水平截面先变大后变小，最后回到原始尺寸，目的是增加石料在800～900℃区域的停留时间。进行截面设计时，首先要考虑石料的堆积角的影响，第一倾斜部210的水平倾斜角α应略小于石料的堆积角；其次，为了不影响石料的下落，要考虑石料的摩擦角的影响，第二倾斜部212的水平倾斜角β应稍微大于石料的摩擦角。
另外，需要说明的是，还可以通过增加预热器高度，即增加环形加热空间20的高度，来做到料面高度可调。
进行预热器设计、制造过程中，增加预热器高度方向上的余量，在实际 生产过程中，可通过改变进、出料量(例如通过调整推杆装置5的运动频率)控制预热器内部环形加热空间20中料层的总高度。增加进料量、减小出料量，将会增加料层总高度，导致料层间隙阻力的增大，烟气流速度减小，进而烟气在环形加热空间20脱硫段内停留时间延长；相反地，减小进料量、增加出料量，将会减小料层总高度，降低料层间隙阻力，烟气流速增加，进而烟气在预热器的脱硫段内停留时间缩短。
本实施方式具有如下优点：
烟气旋流导流喷水装置8安装于排烟管4的入口，此处烟气温度在260～300℃左右，水滴能够吸收烟气的热量而蒸发，同时石灰粉不会因为吸水而变成糊状团聚。而且，因为烟气温度不高，水滴能够停留足够的时间活化脱硫反应；
烟气旋流导流喷水装置8改变烟气进入排烟管4的方式，由原来的轴向进入变为切向进入，烟气、水滴、石灰粉的混合更加均匀、强烈，水滴与烟气的传热传质阻力更小，低温下烟气脱硫效果更好；
由于烟气流的卷吸作用，水滴不会进入预热器的环形加热空间20内，不会影响石灰石在环形加热空间20内的传热传质过程，不会对石灰的生产带来额外的影响；
由于喷水区仅仅存在于烟气旋流导流喷水装置8内部，喷水量可以较少，对烟气温降的影响较小；
改变预热器内壁结构，使烟气与石料在800～900℃区域内即脱硫段停留时间更多，在最优脱硫段停留更多时间，能够显著提升整体的脱硫效率；
在环形加热空间20的高温段固硫剂助剂的添加，改善固硫剂微观孔结构，有利于固硫反应，同时在固硫产物表面覆盖具有高温稳定性的物质，降低固硫产物的再分解，提高固硫产物分解温度；
预热器的环形加热空间20的脱硫段的变截面结构设计，考虑到石料的堆积角以及石料与内板间的摩擦角，石料在下落过程中，能够更好地填充整个预热器的环形加热空间20；
预热器设计、制造时就考虑到料层高度的富余量，实际生产时，根据需要调整预热器进、出料间的平衡，进而调节预热器内部料层高度。
本发明的技术内容及技术特点已揭示如上，然而可以理解，在本发明的创作思想下，本领域的技术人员可以对上述结构作各种变化和改进，包括这里单独披露的或要求保护的技术特征的组合，以及明显地包括这些特征的其它组合。这些变形和/或组合均落入本发明所涉及的技术领域内，并落入本发明权利要求的保护范围。

Claims (10)

  1. 一种具有高效烟气脱硫的回转石灰窑预热器，其包括预热器主体、顶部料仓、下料管、排烟管、推杆装置、下料溜槽，其特征在于还包括固硫剂助剂输送管道，该固硫剂助剂输送管道的下端设置有喷嘴，该喷嘴位于下料溜槽的上方。
  2. 根据权利要求1所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，所述固硫剂助剂输送管道布置在所述预热器主体的中心位置。
  3. 根据权利要求1所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，所述预热器主体包括共同围成环形加热空间的内板和外板，该环形加热空间包括低温段、脱硫段和高温段，该脱硫段设置成由上到下截面先变大再变小以增加物料在该脱硫段内的驻留时间。
  4. 根据权利要求3所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，在所述脱硫段所述内板具有第一倾斜部和第二倾斜部，所述第一倾斜部设置成其水平倾斜角小于物料的堆积角，所述第二倾斜部设置成其水平倾斜角大于物料与所述内板间的摩擦角。
  5. 根据权利要求4所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，所述内板在所述第一倾斜部和所述第二倾斜部之间还设置有竖直部。
  6. 根据权利要求3所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，所述脱硫段的温度设置为800～900℃。
  7. 根据权利要求1至6任一项所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，还包括烟气旋流导流喷水装置，该烟气旋流导流喷水装置装设于所述排烟管的入口端。
  8. 根据权利要求7所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，所述烟气旋流导流喷水装置包括上固定环、下固定板、装设于下固顶板上并朝向所述烟气旋流导流喷水装置内部的喷嘴、与喷嘴连接的水管、固定于上固定环和下固定板之间的多个导流板，该多个导流板围绕所述烟气 旋流导流喷水装置的一个内部假想圆切向分布。
  9. 根据权利要求8所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，所述多个导流板沿着所述内部假想圆切向均匀分布。
  10. 根据权利要求9所述的具有高效烟气脱硫的回转石灰窑预热器，其特征在于，所述内部假想圆的半径为所述排烟管的半径的一半。
PCT/CN2019/115227 2019-02-11 2019-11-04 具有高效烟气脱硫的回转石灰窑预热器 WO2020164259A1 (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201910109617.X 2019-02-11
CN201910109617.XA CN109631593B (zh) 2019-02-11 2019-02-11 具有高效烟气脱硫的回转石灰窑预热器

Publications (1)

Publication Number Publication Date
WO2020164259A1 true WO2020164259A1 (zh) 2020-08-20

Family

ID=66065143

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2019/115227 WO2020164259A1 (zh) 2019-02-11 2019-11-04 具有高效烟气脱硫的回转石灰窑预热器

Country Status (2)

Country Link
CN (1) CN109631593B (zh)
WO (1) WO2020164259A1 (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116332667A (zh) * 2023-04-06 2023-06-27 中国科学院过程工程研究所 一种含硫固废制备多孔材料及固化硫的方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109631593B (zh) * 2019-02-11 2023-09-26 江苏中圣园科技股份有限公司 具有高效烟气脱硫的回转石灰窑预热器

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102974207A (zh) * 2012-11-07 2013-03-20 环境保护部华南环境科学研究所 用于水泥回转窑烟气同时脱硝脱硫的方法及装置
CN103896501A (zh) * 2013-12-30 2014-07-02 辽宁劲达华杰工程技术有限公司 一种石灰生产线窑尾通风系统及窑尾通风工艺
WO2016155236A1 (zh) * 2015-04-03 2016-10-06 石家庄新华能源环保科技股份有限公司 一种间壁式回转窑装置
CN205760546U (zh) * 2016-05-12 2016-12-07 南京凯盛国际工程有限公司 水泥窑脱硫系统
CN206138996U (zh) * 2016-09-19 2017-05-03 中材国际环境工程（北京）有限公司 一种新型水泥窑半干法脱硫系统
CN107754591A (zh) * 2017-11-20 2018-03-06 上海三融环保工程有限公司 一种高效雾化脱硫装置及方法
CN107930376A (zh) * 2017-11-27 2018-04-20 浙江工业大学 一种干湿结合的水泥窑脱硫装置及工艺
CN108686494A (zh) * 2018-06-21 2018-10-23 北京中丹科技有限公司 用窑尾烟气中的氧化钙对窑尾烟气脱硫的方法及其系统
CN109631593A (zh) * 2019-02-11 2019-04-16 江苏中圣园科技股份有限公司 具有高效烟气脱硫的回转石灰窑预热器
CN209512528U (zh) * 2019-02-11 2019-10-18 江苏中圣园科技股份有限公司 具有高效烟气脱硫的回转石灰窑预热器

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20040007880A (ko) * 2002-07-11 2004-01-28 주식회사 포스코 로내 열가스 제어 시스템을 구비한 회전식 소성로
JP3759116B2 (ja) * 2003-03-28 2006-03-22 株式会社プランテック 廃棄物焼却用竪型ごみ焼却炉及びその制御方法
CN104651564B (zh) * 2015-02-13 2017-01-04 唐竹胜 一种低温快速还原分离粒铁的方法
CN104876456B (zh) * 2015-05-16 2017-07-11 江苏中圣园科技股份有限公司 回转窑石灰焙烧工艺
CN107174927A (zh) * 2017-07-13 2017-09-19 北京建筑材料科学研究总院有限公司 一种水泥回转窑的脱硝方法和系统

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102974207A (zh) * 2012-11-07 2013-03-20 环境保护部华南环境科学研究所 用于水泥回转窑烟气同时脱硝脱硫的方法及装置
CN103896501A (zh) * 2013-12-30 2014-07-02 辽宁劲达华杰工程技术有限公司 一种石灰生产线窑尾通风系统及窑尾通风工艺
WO2016155236A1 (zh) * 2015-04-03 2016-10-06 石家庄新华能源环保科技股份有限公司 一种间壁式回转窑装置
CN205760546U (zh) * 2016-05-12 2016-12-07 南京凯盛国际工程有限公司 水泥窑脱硫系统
CN206138996U (zh) * 2016-09-19 2017-05-03 中材国际环境工程（北京）有限公司 一种新型水泥窑半干法脱硫系统
CN107754591A (zh) * 2017-11-20 2018-03-06 上海三融环保工程有限公司 一种高效雾化脱硫装置及方法
CN107930376A (zh) * 2017-11-27 2018-04-20 浙江工业大学 一种干湿结合的水泥窑脱硫装置及工艺
CN108686494A (zh) * 2018-06-21 2018-10-23 北京中丹科技有限公司 用窑尾烟气中的氧化钙对窑尾烟气脱硫的方法及其系统
CN109631593A (zh) * 2019-02-11 2019-04-16 江苏中圣园科技股份有限公司 具有高效烟气脱硫的回转石灰窑预热器
CN209512528U (zh) * 2019-02-11 2019-10-18 江苏中圣园科技股份有限公司 具有高效烟气脱硫的回转石灰窑预热器

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116332667A (zh) * 2023-04-06 2023-06-27 中国科学院过程工程研究所 一种含硫固废制备多孔材料及固化硫的方法

Also Published As

Publication number Publication date
CN109631593B (zh) 2023-09-26
CN109631593A (zh) 2019-04-16

Similar Documents

Publication Publication Date Title
CA2935621C (en) Process and apparatus for dry granulation of slag with reduced formation of slag wool
WO2020164259A1 (zh) 具有高效烟气脱硫的回转石灰窑预热器
KR101911213B1 (ko) 순환 유동층 보일러 플랜트로부터 나오는 연도 가스의 이산화황 함량을 감소시키는 방법
EP3099398B1 (en) A method of and a scrubber for removing pollutant compounds from a gas stream
CN108525508A (zh) 利用水泥生料进行烟气脱硫的方法
CN110180349A (zh) 一种链篦机-回转窑球团烟气超低排放系统
CN101385941B (zh) 高效循环流化床烟气脱硫装置
CN106178907A (zh) 一种循环流化床锅炉超细脱硫剂颗粒脱硫方法
CN104548920B (zh) 一种脱硫装置及脱硫方法
RU2283816C2 (ru) Способ и установка для производства цементного клинкера
CN104876596B (zh) 一种氧化锆质定径水口的制备方法及设备
CN106268282B (zh) 循环流化床烟气脱硫装置
CN217220890U (zh) 优化的生活垃圾焚烧烟气脱硝脱酸除尘一体化系统
CN105126563B (zh) 一种玻璃熔窑烟气的脱硫脱硝介质及脱硫脱硝设备和方法
CN107596878B (zh) 一种循环流化床锅炉炉内脱硫方法
CN209512528U (zh) 具有高效烟气脱硫的回转石灰窑预热器
JPS6325403A (ja) 煙道ガス中の二酸化硫黄含有量を低減する燃焼方法ならびに装置
CN204261558U (zh) 一种脱硫装置
CN212283543U (zh) 一种干法烟气脱硫装置
CN101780370B (zh) 基于内循环w型多流体碱雾发生器的脱硫装置及脱硫方法
CN113117490A (zh) 烟气脱硫脱硝和胶凝材料生产的一体化工艺
CN205127701U (zh) 一种玻璃熔窑烟气的脱硫脱硝设备
CN109731396B (zh) 一种制备辊道窑除尘用滤料混合流化床
CN109731397B (zh) 一种混合流化床制备辊道窑除尘用滤料方法
CN101619856A (zh) 一种锅炉烟气净化方法

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: 19914975

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: 19914975

Country of ref document: EP

Kind code of ref document: A1

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205A DATED 08/03/2022)

122 Ep: pct application non-entry in european phase

Ref document number: 19914975

Country of ref document: EP

Kind code of ref document: A1