KR102330077B1 - Cement manufacturing devices and methods for reducing NOx by applying real-time analysis and low NOx combustion and post-processing technology - Google Patents

Abstract

The present invention applies a low NOx combustion technology, a high-efficiency advanced SNCR technology, and a multi-material analysis technology to apply a real-time analysis and low NOx combustion and post-treatment technology that can effectively suppress NOx generation during the pre-treatment and post-treatment of the cement production process. It relates to a cement manufacturing apparatus and method with reduced

Description

Cement manufacturing devices and methods for reducing NOx by applying real-time analysis and low NOx combustion and post-processing technology

The present invention relates to an apparatus and method for manufacturing cement with reduced NOx by applying real-time analysis and low NOx combustion and post-treatment technology. In more detail, by applying low NOx combustion technology, high-efficiency advanced SNCR technology, and multi-material analysis technology, real-time analysis and low NOx combustion and post-treatment technology that can effectively suppress NOx generation during pre-treatment and post-treatment of the cement production process are applied. It relates to an apparatus and method for manufacturing cement with reduced NOx.

The cement clinker production plant comprises a clinker kiln, the output end of the clinker kiln connected to a clinker cooler, the supply end of the clinker kiln connected to a preheater and optionally a calciner, said preheater being connected to at least a plurality of in series It comprises two cyclone suspension type heat exchangers through which the kiln flue-gas can flow continuously along a flow path, in which the raw material is preheated in stages.

In the manufacture of such cement clinker, the raw material is preheated, completely dried, calcined and burned into clinker, followed by cooling. Plants operated according to this drying procedure include preheaters, calciners, tertiary air ducts, rotary kilns and clinker coolers included in heat exchangers of the cyclone suspension type.

The energy required for material conversion to cement in these plants is provided by supplying fuel for combustion to rotary kilns and calciners. The air heated in the clinker cooler is supplied partly to the rotary kiln as so-called secondary air and partly to the calcination furnace as so-called tertiary air.

The flue-gases of the rotary kiln are directed to and flow through the calciner through a kiln feed chamber and a flow contraction provided thereon, are produced in the calciner and smoke gas from calciner fuel and carbon dioxide. It is discharged into the preheater together with the exhaust gases constituting the smoke gas.

The cement produced in this way is produced by mixing clay and iron oxide with limestone as the main raw material, calcining and sintering at high temperature to produce clinker, and adding gypsum to it to finely pulverize it.

In addition, the process that affects the exhaust gas component including nitrogen oxide during the process is calcining (800 ~ 1200 ℃), sintering (Sintering, Max. 1800 ℃) process.

US Patent Publication No. 2014/0178271 discloses a technology for suppressing NOx generation through the supply fraction of fuel supplied to the calcination and sintering unit and the hot air supplied to the cooler and the sintering unit.

In Korean Patent Laid-Open Publication No. 2003-0079666, the selective non-catalytic reduction method (SNCR) injecting urea injects ammonia and urea according to the combustion temperature and the amount of nitrogen oxide generated by a sprayer disposed at the opening of the kiln, and the reducing agent is injected. A technique is disclosed for circumferentially disposing a plurality of atomizers at a temperature point suitable for the reaction of the urea in the calciner and cyclone in the city.

WO 2009/034626 discloses a flow path for solid powder fuel provided with a plurality of flow paths divided by a plurality of concentric cylindrical members, and a flow path for solid powder fuel provided with a turning means for solid powder fuels, and disposed on the outside adjacent to the flow path, , a first air flow path having means for turning the air flow, a second air flow passage disposed on the outside adjacent to the flow passage, and an inner side disposed adjacent to the flow passage for solid powder fuel, the air flow turning means being provided Disclosed is a technique for specifying a turning angle of each air flow path including a third air flow path.

In WO 2012/114645, the reaction rate of each difference is measured in advance for a plurality of types of pulverized coal, and the relationship between the NOX concentration in the exhaust gas and the reaction rate is obtained, and based on the relationship, A technique is disclosed in which the pulverized coal of the plurality of coal types is blended and supplied as a fuel of the combustion facility so that the reaction rate of the vehicle becomes a value corresponding to the target NOx concentration or less.

In Japanese Patent Registration No. 6330352, a pulverized coal burner for supplying pulverized coal, a waste plastic input port for inputting waste plastic, and an oxygen supply port for supplying oxygen are provided. A cement calciner technology is disclosed in which the waste plastic inlet forms a swirling flow formed separately from the pulverized coal burner and the oxygen supply port.

However, there is no case of presenting a technology for a cement manufacturing apparatus and method containing waste plastic as a fuel by applying a low NOx combustion technology, an improved SNCR technology, and a real-time multi-exhaust gas monitoring technology.

US Patent Publication No. 2014/0178271 Korean Patent Publication No. 2003-0079666 WO 2009/034626 Publication No. WO Patent Publication No. 2012/114645 Japanese Patent No. 6330352

The present invention is intended to solve the above problems, and real-time analysis and real-time analysis that can effectively suppress NOx generation during pre-treatment and post-treatment of the cement production process by applying low NOx combustion technology, high-efficiency advanced SNCR technology, and multi-material analysis technology An object of the present invention is to provide an apparatus and method for manufacturing cement with reduced NOx by applying low NOx combustion and post-treatment technology.

인 영역에 요소수를 분무하는 하나 이상의 요소수분무기가 형성되며, 상기 요소수분문기가 형성된 영역은 공기 대비 연료비(Air/Fuel ratio)가 1보다 작은 영역이고, 상기 예열유닛과 상기 하소유닛 사이에는 NO, NH3 및 온도를 실시간으로 측정할 수 있는 레이저측정유닛;을 포함하는 NOx 발생을 억제하기 위한 시멘트 제조 시스템을 제공할 수 있다.The present invention for achieving this object is a cement manufacturing system for suppressing NOx generation, comprising: a fuel input unit 100 for inputting fuel; one or more preheating units 200 communicating with the fuel input unit to preheat and discharge the fuel; a calcining unit 300 communicating with the preheating unit to calcinate and discharge the fuel; a sintering unit 400 communicating with the calcining unit to sinter the fuel and discharge it as clinker; and a cooling unit 500 communicating with the sintering unit to cool and discharge the clinker, and the calcination combustor formed in the calcination unit includes a reburning area, and the temperature of the calcination unit is 900 to 1100.

One or more urea water atomizers for spraying urea water are formed in the phosphorus area, and the area where the urea water meter is formed is an area where the air/fuel ratio is less than 1, and between the preheating unit and the calcining unit It is possible to provide a cement manufacturing system for suppressing NOx generation, including; a laser measurement unit capable of measuring NO, NH3 and temperature in real time.

이하 저온영역투입비(W_L)/ W_U)는 0.01 내지 0.99일 수 있다.In addition, 900 to 1000 relative to the _{total weight (W U} ) of the urea water sprayed through the urea water sprayer

Hereinafter, the low-temperature region input ratio (W _L )/W _U ) may be 0.01 to 0.99.

이하 고온영역투입비(W_H)/ W_U)는 0.01 내지 0.99일 수 있다.In addition, in excess of 1000 to 1100 compared to the total weight (Wu) of the urea water sprayed through the urea water sprayer

Hereinafter, the high-temperature region input ratio (W _H )/W _U ) may be 0.01 to 0.99.

In addition, the amount of calcium oxide (CaO) included in the unit air amount supplied to the calcination unit (g/Nm ³ ) may be 0 to 0.5 or less.

In addition, at least one sinter combustor formed in the calcination combustor and/or the sintering unit may be formed, and the fuel of the at least one calcination combustor and/or the sinter combustor may be waste plastic.

In addition, the combustor 310 using the waste plastic as a fuel includes: a first fuel injection unit 311 into which the waste plastic is injected; A first oxygen supply unit in communication with the first fuel injection unit 311 and in which primary combustion air of 10 to 35% of the total amount of oxygen supplied to the combustor is supplied in a straight direction such as the axial direction of the combustor 310 . (321); A first air injection unit 312 in which air for transporting waste plastic is supplied, and the supplied air is supplied as air containing 5 to 15% of the total amount of oxygen supplied to the combustion furnace; a second oxygen supply unit 322 communicating with the first air injection unit 312 and supplying secondary oxygen of 10 to 40% of the total amount of oxygen supplied to the combustion furnace; a third oxygen supply unit 323 connected to the first air injection unit 312 and supplied with tertiary oxygen of 35 to 65% of the total amount of oxygen supplied to the combustion furnace; and a turning part 330 provided at the ends of the second oxygen supply part 322 and the third oxygen supply part 323 so that the secondary and tertiary oxygen are supplied to the calcination unit in a swirling flow. and the first fuel injection part 311 , the injection pipe of the first oxygen supply part 321 , the first air injection part 312 , the injection pipe of the second oxygen supply part 322 , and the third oxygen The injection pipe of the supply part 323 is coaxial with each inner diameter sequentially increasing, and each interval between the outer peripheral surface and the inner peripheral surface of each injection tube is wider toward the outside of the combustor, and the combustor is supplied to the calcination unit. At least one is formed in a tangential direction with respect to the cross-section of the calcination unit, and is formed upward at 10 degrees or more and 60 degrees or less based on the cross-section to increase the residence time of the injected waste plastic to additionally secure combustion time. can

In addition, between the preheating unit and the calcination unit PM 1 to 2.5 or less ultra-fine particle analysis unit; may further include.

In addition, the laser measuring unit includes a laser light source for irradiating a laser; a chamber in which a gas for temperature or concentration measurement is disposed; a reflection unit which reflects the laser irradiated from the laser light source unit and is disposed so that the trajectory of the reflected laser can pass through the chamber at least once; a photodetector disposed at the distal end of the laser trajectory reflected by the reflector and condensing the laser; A laser detection system comprising a; a processor for performing analysis using the laser detected by the photodetector, comprising: at least one sound wave generator positioned on one surface of the chamber; and at least one reflector located on the other surface of the chamber facing the at least one sound wave generator, wherein the sound wave generator may be driven to create a multidimensional standing acoustic wave in the chamber.

As described above, the NOx-reduced cement manufacturing apparatus and method to which the low NOx combustion technology and improved SNCR are applied has the effect of reducing nitrogen oxides through precise monitoring and analysis of the downstream process.

In addition, there is an effect of facility improvement because it does not require the addition of an additional nitrogen oxide removal catalyst and equipment.

1 is a structural diagram of a conventional cement manufacturing process system.
2 is a conceptual diagram of a cement manufacturing process system according to an embodiment of the present invention.
3 is a structural diagram of a cement manufacturing process combustor according to an embodiment of the present invention.
4 is a graph of NOx removal efficiency according to the CaO content of the cement manufacturing process according to an embodiment of the present invention.

Hereinafter, embodiments in which those of ordinary skill in the art to which the present invention pertains can easily practice the present invention will be described in detail with reference to the accompanying drawings. However, in the detailed description of the principle of operation of the preferred embodiment of the present invention, if it is determined that a detailed description of a related known function or configuration may unnecessarily obscure the subject matter of the present invention, the detailed description thereof will be omitted.

In addition, the same reference numerals are used throughout the drawings for parts having similar functions and functions. Throughout the specification, when a part is said to be connected to another part, this includes not only a case in which it is directly connected, but also a case in which it is indirectly connected with another element interposed therebetween. In addition, the inclusion of a certain component does not exclude other components unless otherwise stated, but means that other components may be further included.

Hereinafter, the present invention will be described in more detail.

1 is a structural diagram of a conventional cement manufacturing process system.

A cement clinker manufacturing system in which the raw meal charged is preheated in a preheater counter-current to the hot flue-gases of the clinker kiln and calcined in a calciner.

The clinker exits through the back end of the clinker kiln and is cooled in a clinker cooler. The cooled clinker is cooled through the injected cooling air and then exits through the rear end of the clinker cooler.

The preheater may comprise one or several preheaters. The batch of preheaters may comprise a plurality of continuously arranged cyclone suspension-type heat exchangers.

The suspension type heat exchanger is connected in succession to the last suspended heat exchanger and may consist of intermediately arranged suspension type heat exchangers.

The air blower fed to the kiln can create the required negative pressure to draw the kiln flue-gases appearing on the hot raw feed side of the clinker kiln through the calciner and continuously arranged suspension type heat exchangers as well as hot gas flues. .

Air for sintering fuel and oxidant in the clinker kiln can be supplied. A fuel supply for the calcination system of the calciner may be formed on one side of the calciner.

The clinker cooler includes a plurality of blowers, through which air is blown into the air. Air passes through the clinker cooler and can be introduced from the clinker cooler into the calcination furnace through tertiary air vents and tertiary air channels, tertiary air channel openings.

In addition to the hot gas flue, the kiln flue gas can also be withdrawn via a branch duct, the branch point being located on the outlet of the heat exchanger of the uppermost first suspension type.

A control organ constituting a valve in the branch duct can be formed, which valve can regulate the amount of kiln flue gas drawn out.

The exiting kiln flue-gas is fed to a mixing device, such as a mixing cyclone, where a portion of the converted kiln flue-gas is exhausted through the hot gas flue and mixed with the remaining kiln flue-gas exhausted through the entire preheater. The raw material for the clinker is heated in a calciner at a temperature of 700 to 900° C., in particular 850° C., with a temperature of about 850° C. by means of a part of the kiln flue-gas withdrawn via a branch duct.

The residual amount of the kiln flue-gas passed through the preheater has a temperature of 250 to 350° C., in particular 300° C. in the hot gas flue. The hot gas exiting the mixing device has a temperature of 400 to 550° C. depending on the volume ratio of the flue gas streams. Thereafter, the hot gas may be supplied to a dedusting device through a duct, and the dedusting hot gas may be input for drying the raw material.

Additionally hot gas may be supplied via a duct to a coal grinder for drying coal provided as fuel for the firing system.

2 of FIG. 2 is a conceptual diagram of a cement manufacturing process system according to an embodiment of the present invention.

A cement manufacturing system for suppressing NOx generation, comprising: a fuel input unit (100) for inputting fuel; one or more preheating units 200 communicating with the fuel input unit to preheat and discharge the fuel; a calcining unit 300 communicating with the preheating unit to calcinate and discharge the fuel; a sintering unit 400 communicating with the calcining unit to sinter the fuel and discharge it as clinker; and a cooling unit 500 communicating with the sintering unit to cool and discharge the clinker, and the calcination combustor 310 formed in the calcination unit includes a reburning area, and the temperature of the calcination unit is One or more urea water sprayers 340 for spraying urea water in an area of 900 to 1100° C. are formed, and the area in which the urea water sprayer is formed has an air/fuel ratio less than 1, and the preheating Between the unit and the calcination unit, it is possible to provide a cement manufacturing system for suppressing NOx generation, including a laser measuring unit 600 capable of measuring _{NO, NH 3 and temperature in real time.}

The laser measuring unit includes a laser light source for irradiating a laser, a chamber in which a gas for measuring temperature or concentration is disposed, and a trajectory of the reflected laser by reflecting the laser irradiated from the laser light source so that the trajectory of the reflected laser can pass through the chamber more than once. A laser detection system comprising a; a reflector disposed at the end of the laser trajectory reflected by the reflector, a photodetector for condensing the laser, and a processor for performing analysis using the laser detected by the photodetector In the following, at least one sound wave generator positioned on one surface of the chamber, and at least one reflector positioned on the other surface of the chamber facing the at least one sound wave generator, wherein the sound wave generator provides a multi-dimensional sound to the chamber. It can be driven to create a standing wave.

The improved SNCR technology should induce short-time complete mixing by applying a high-pressure nozzle to improve the spray nozzle and optimize the reaction, and optimize the balance between the rapid reaction and the injection momentum in consideration of the reaction time and uniform distribution. For the improved SNCR, the conditions for spraying the reducing agent at the optimal location should be designed in consideration of the reaction temperature, residence time, flue gas flow rate, and concentration. In addition, it should be designed to minimize the reducing agent injection field and CaO dust through mutual optimization with SNCR linked with combustion conditions. Considering the change in CO concentration, additional air can be added.

The urea water sprayer may have a porous body formed in a pipe into which the urea water and additives are injected.

The porous body may be for mixing and heating the urea water and the additive.

The porous body may be associated with a heating unit for heating to a predetermined temperature.

Instead of the porous body, an x-vane may be formed on the conduit.

The urea water atomizer may have a spray nozzle formed at the spray end, a urea water spray tube may be connected to the center, and an air tube may be formed in an annular shape of the urea water spray tube.

The urea water sprayer can implement micro-droplets of urea water in an electro-spraying type, not in a physical form.

_{The low-temperature region input ratio (W L} )/W _U ) of 900 to 1000° C. or less relative to the total weight of urea water sprayed through the urea water sprayer (W _U ) may be 0.01 to 0.99.

The low-temperature region input ratio (W _L )/W _U may be 0.01 to 0.99, preferably 0.3 to 0.8, and more preferably 0.4 to 0.6. If it is out of the low-temperature region input ratio, a smooth NOx removal reaction efficiency cannot be obtained.

이하 고온영역투입비(W_H)/W_U)는 0.01 내지 0.99일 수 있다. Exceeding 1000 to 1100 based on the total weight (Wu) of the number of urea sprayed through the urea water sprayer

Hereinafter, the high-temperature region input ratio (W _H )/W _U ) may be 0.01 to 0.99.

The high-temperature region input ratio (W _H )/W _U may be 0.01 to 0.99, preferably 0.3 to 0.8, and more preferably 0.4 to 0.6. If it is out of the high-temperature region input ratio, a smooth NOx removal reaction efficiency cannot be obtained.

^{The amount (g/Nm 3} ) of calcium oxide (CaO) included in the unit air amount supplied to the calcination unit may be 0 to 0.5 or less.

As the calcium oxide dust introduced from the preheater and the pre-firing device passes through the SNCR process, there is a problem that the efficiency of the SNCR decreases. _{The decrease in the denitration efficiency of NH 3} by calcium oxide is due _{to a chemical reaction in which NH 3} is _{decomposed into N 2} on the surface of the calcium oxide particles, and may cause a rapid decrease in the denitration efficiency.

At least one sinter combustor formed in the calcination combustor and/or the sintering unit may be formed, and the fuel of the at least one calcination combustor and/or the sinter combustor may be waste plastic.

3 is a structural diagram of a cement manufacturing process combustor according to an embodiment of the present invention.

정도이며, 전체 공정 중의 약 50%의 에너지를 사용한다. 제품 품질과 직결되는 소성로(킬른로)에 비해, 온도 및 공연비 유동성이 크면서도 에너지를 많이 사용하므로, 저 NOx를 위한 기술적용 및 최적화가 용이하다. The calcination process is a process of separating calcium oxide (CaO) and carbon dioxide (CO2) by applying heat to limestone (CaCO3) before the sintering process in which clinker is generated. The temperature of the calciner is 800-1200.

It uses about 50% of the energy of the whole process. Compared to a kiln (kiln furnace) that is directly related to product quality, it uses a lot of energy while having a high temperature and air-fuel ratio fluidity, so it is easy to apply and optimize technology for low NOx.

The low NOx combustion technology that can be applied to the combustor of the calcination furnace has a long reaction time because the fuel is a solid fuel, so a sufficient residence time must be secured. ask for Therefore, it is necessary to review the supply with the appropriate air ratio controlled for each stage in consideration of the homogeneous mixture of fuel and air, volatile combustion and char combustion.

As the calcination, reburning may be applied. In order to reduce NOx generated in the kiln furnace, it can be reduced by reducing _{NO to N 2} in the fuel rich state at the beginning of the calcination furnace after the kiln furnace. It is self-evident that all hydrocarbons such as coal and waste can be reburned fuel.

Additionally, multistaged combustion may be applied. The fuel/air input ratio can be adjusted, the air-fuel ratio and temperature can be controlled, and multi-stage combustion technology can be applied in consideration of the calorific value and reaction speed for each input fuel. In particular, the combustor dedicated to the calcination furnace is developed with a low NOx combustor with high single flame and load variation characteristics, considering the conditions of the calcination furnace, and can mix coal and waste as fuel.

It affects the heat transfer to the raw material in a reducing atmosphere, the decarboxylation characteristics and the cement mineral phase formation characteristics. By calculating the optimal distribution of mixed raw materials, fuel, and combustion air for cement manufacturing, it is necessary to design the conditions for complete combustion of the used fuel, optimal heat transfer conditions between the fuel and the mixed raw materials, and the calcination of the mixed raw materials.

The combustor 310 using the waste plastic as a fuel includes: a first fuel injection unit 311 into which the waste plastic is injected; A first oxygen supply unit in communication with the first fuel injection unit 311 and in which primary combustion air of 10 to 35% of the total amount of oxygen supplied to the combustor is supplied in a straight direction such as the axial direction of the combustor 310 . (321); A first air injection unit 312 in which air for transporting waste plastic is supplied, and the supplied air is supplied as air containing 5 to 15% of the total amount of oxygen supplied to the combustion furnace; a second oxygen supply unit 322 communicating with the first air injection unit 312 and supplying secondary oxygen of 10 to 40% of the total amount of oxygen supplied to the combustion furnace; a third oxygen supply unit 323 connected to the first air injection unit 312 and supplied with tertiary oxygen of 35 to 65% of the total amount of oxygen supplied to the combustion furnace; and a turning part 330 provided at the ends of the second oxygen supply part 322 and the third oxygen supply part 323 so that the secondary and tertiary oxygen are supplied to the calcination unit in a swirling flow. and the first fuel injection part 311 , the injection pipe of the first oxygen supply part 321 , the first air injection part 312 , the injection pipe of the second oxygen supply part 322 , and the third oxygen The injection pipe of the supply part 323 is coaxial with each inner diameter sequentially increasing, and each interval between the outer peripheral surface and the inner peripheral surface of each injection tube is wider toward the outside of the combustor, and the combustor is supplied to the calcination unit. At least one is formed in a tangential direction with respect to the cross-section of the calcination unit, and is formed upward at 10 degrees or more and 60 degrees or less based on the cross-section to increase the residence time of the injected waste plastic to additionally secure combustion time. can

The combustor may be applied to the combustor of the sintering unit, and a plurality of combustors may be formed.

Between the preheating unit and the calcination unit PM 1 to 2.5 or less ultra-fine particle analysis unit; may further include.

The ultrafine particles may be reaction byproducts generated in the SNCR process.

The ultra-fine particles are _{corrosive as SO 3} and rebound with water to cause flow path contamination and corrosion.

CaSO ₄ is produced by the reaction of CaO and SO _{3 .} In SCR, it causes clogging of the pores of the catalyst, and in SNCR, fine dust is generated and reacts with various by-products, which can become the cause of flow path adsorption.

(NH ₄ )HSO ₄ is an acidic substance and causes flow path contamination and corrosion.

(NH ₄ ) ₂ SO ₄ is fine particles with a diameter of ~3 ㎛ or less and is the cause of visible soot (ultra-fine dust).

Unreacted ammonia itself is a toxic substance and forms ammonium salts such as _{NH 4} NO ₃ and (NH ₄ )NSO ₄ at low temperatures with _{moisture, SO 2 , and NOx.} can be

Compounds of alkali metals and other metals are: responsible for flow path adsorption and fine particles.

The ultrafine particle analysis unit may be a surface plasmone enhanced Raman Spectroscopy (SERS).

Multiple analysis of generated chemical species is required for process maintenance, and 2D tomography for ununiform cross-sectional analysis can be obtained by linking _{real-time NO and NH 3 monitoring and combustion and SNCR control.} The above measurement principle is based on the Lambert-Beer law.

As described above in detail specific parts of the present invention, for those of ordinary skill in the art, these specific descriptions are only preferred embodiments, and the scope of the present invention is not limited thereby, It is obvious to those skilled in the art that various changes and modifications can be made within the scope and spirit of the present invention, and it is natural that such variations and modifications fall within the scope of the appended claims.

100: fuel input unit
200: preheating unit
300: calcination unit
310: calcination combustor
311; 1st fuel injection part
312: first air injection unit
321: first oxygen supply unit
322: second oxygen supply unit
323: third oxygen supply unit
330: turning
340: urea water atomizer
400: sintering unit
500: cooling unit
600: laser measuring unit

Claims (8)

In the cement manufacturing system for suppressing NOx generation,
a fuel input unit 100 for inputting fuel;
one or more preheating units 200 communicating with the fuel input unit to preheat and discharge the fuel;
The calcination unit 300 communicates with the preheating unit to calcinate and discharge the fuel.
The sintering unit 400 communicates with the calcination unit to sinter the fuel and discharge it as clinker.
and a cooling unit 500 communicating with the sintering unit to cool and discharge the clinker,
The calcination combustor formed in the calcination unit includes a reburning area,
One or more urea water sprayers for spraying urea water in an area where the temperature of the calcination unit is 900° C. to 1100° C. or less is formed,
The area in which the urea water atomizer is formed is an area in which the air/fuel ratio is less than 1,
A laser measuring unit capable of measuring _{NO, NH 3} and temperature in real time between the preheating unit and the calcining unit;
Cement manufacturing system to suppress NOx generation.
The method according to claim 1
The ratio (W _L /W _{U ) of the low-temperature region input (W L} ) of 900 ° C to 1000 ° C or less relative _{to the total weight (W U} ) of the urea water sprayed through the urea water sprayer is 0.01 or more to 0.99 or less,
Cement manufacturing system to suppress NOx generation.
The method according to claim 1
The ratio (W _H /W _{U ) of the input amount (W H} ) of the high temperature region exceeding 1000 ° C to 1100 ° C or less relative to the total weight (Wu) of the urea water sprayed through the urea water sprayer is 0.01 or more to 0.99 or less,
Cement manufacturing system to suppress NOx generation.
The method according to claim 1
The amount of calcium oxide (CaO) included in the unit air amount supplied to the calcination unit (g/Nm ³ ) is a cement production system for suppressing the generation of NOx in the range of more than 0 to 0.5 or less.
According to claim 1,
At least one sintering combustor formed in the calcination combustor and the sintering unit may be formed,
A cement manufacturing system for suppressing generation of NOx, wherein the fuel of the at least one calciner and the sinter combustor is a waste plastic.
6. The method of claim 5,
The combustor 310 using the waste plastic as fuel,
a first fuel injection unit 311 into which waste plastic is injected;
A first oxygen supply unit in communication with the first fuel injection unit 311 and in which primary combustion air of 10 to 35% of the total amount of oxygen supplied to the combustor is supplied in a straight direction, such as the axial direction of the combustor 310 . (321);
A first air injection unit 312 in which air for transporting waste plastic is supplied, and the supplied air is supplied as air containing 5 to 15% of the total amount of oxygen supplied to the combustion furnace;
a second oxygen supply unit 322 communicating with the first air injection unit 312 and supplying secondary oxygen of 10-40% of the total amount of oxygen supplied to the combustor;
a third oxygen supply unit 323 communicating with the first air injection unit 312 and supplying 35 to 65% tertiary oxygen of the total amount of oxygen supplied to the combustor; and
and a turning part 330 provided at the ends of the second oxygen supply part 322 and the third oxygen supply part 323 so that the secondary and tertiary oxygen are supplied to the calcination unit in a swirling flow; and ,
The first fuel injection part 311, the injection pipe of the first oxygen supply part 321, the first air injection part 312, the injection pipe of the second oxygen supply part 322, the third oxygen supply part ( 323) is coaxial with each inner diameter sequentially increasing, and each interval between the outer peripheral surface and the inner peripheral surface of each injection tube is wider toward the outside of the combustor,
One or more combustors supplied to the calcination unit are formed in a tangential direction with respect to the cross section of the calcination unit,
It is formed in the upper direction at 10 degrees or more and 60 degrees or less based on the cross-sectional image to increase the residence time of the sprayed waste plastic to additionally secure the combustion time.
Cement manufacturing system to suppress NOx generation.
According to claim 1,
A cement manufacturing system for suppressing the generation of NOx further comprising; an ultrafine particle analysis unit of PM 1 to 2.5 or less between the preheating unit and the calcining unit.
According to claim 1,
The laser measuring unit is
A laser light source for irradiating a laser;
a chamber in which a gas for temperature or concentration measurement is disposed;
a reflection unit which reflects the laser irradiated from the laser light source unit and is disposed so that the trajectory of the reflected laser can pass through the chamber at least once;
a photodetector disposed at the distal end of the laser trajectory reflected by the reflector and condensing the laser;
In the laser detection system comprising a; a processor for performing analysis using the laser detected by the photodetector,
at least one sound wave generator positioned on one surface of the chamber;
and at least one reflector located on the other surface of the chamber facing the at least one sound wave generator, wherein the sound wave generator is driven to create a multidimensional acoustic standing wave in the chamber.

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