CN102923979A - Clinker production line for novel dry process cement kiln and denitration process method for clinker production line - Google Patents
Clinker production line for novel dry process cement kiln and denitration process method for clinker production line Download PDFInfo
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- CN102923979A CN102923979A CN2012103983053A CN201210398305A CN102923979A CN 102923979 A CN102923979 A CN 102923979A CN 2012103983053 A CN2012103983053 A CN 2012103983053A CN 201210398305 A CN201210398305 A CN 201210398305A CN 102923979 A CN102923979 A CN 102923979A
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- 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
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- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
- Y02P40/121—Energy efficiency measures, e.g. improving or optimising the production methods
Abstract
The invention discloses a clinker production line for a novel dry process cement kiln. Pulverized coal in a pulverized coal pipeline which is communicated with the tail of the kiln is divided into two channels by a first pulverized coal distributor, wherein one channel is communicated with a column body on the upper part of a decomposition furnace, and the pulverized coal is divided into two channels again by a second pulverized coal distributor and symmetrically enters the column body on the upper part of the decomposition furnace; and the other channel is communicated with a cone on the lower part of the decomposition furnace, and the pulverized coal is divided into two channels again by the second pulverized coal distributor and symmetrically enters the cone on the lower part of the decomposition furnace. The invention also provides a denitration process method adopted by the production line. By the technical scheme, thermal NOx generated in the kiln is decreased and reduced, and the generation of fuel NOx is inhibited, so that NOx can be effectively reduced from the source; and after process improvement, operation parameters are optimized, the operation quality and stability of the system are promoted, and a certain energy-saving effect is achieved.
Description
Technical field
The invention belongs to the technical field of manufacture of cement, relate to the production technology of new dry process rotary kiln, more particularly, the present invention relates to a kind of new dry process rotary kiln clinker production line, in addition, the invention still further relates to the denitrating technique method of this production line.
Background technology
One, cement clinker production line denitration technology background:
At present, China has nearly 5000 of cement production enterprise, and output occupies first place, the world for years.Whole nation accumulative total cement total output was 20.9 hundred million tons in 2011, and wherein, new type nonaqueous cement proportion reaches 80.9%.End the end of the year in 2011, adopt the new type nonaqueous cement production line of domestic technique and equipment build-up to reach more than 1500.
The reduction of discharging problem of oxynitride has become the significant problem of restriction China's environment and Economic development.Along with country formally brings the reduction of oxynitride into schedule, relevant departments have put into effect policy and the pollutant emission standard of a series of manufacture of cement NOx emission controls in succession.
National cement industry discharging NOx was about 2,000,000 tons in 2010, account for about 10% of industrial source total emission volumn, be only second to electric power and automotive emission, occupy the 3rd, so the emission reduction work of cement industry oxynitride occupies very important status in China's oxynitride overall control.
Two, the mechanism of production of cement clinker production line NOx and position:
The NOx of New Style of Dry Cement Kiln system production ways mainly contains three kinds of heating power type, fuel type and Quick-type NOx etc., and the principle of its generation, position and generation situation analysis are as follows:
1, " heating power type " NOx:
Airborne N
2At high temperature oxidation and the NOx that produces, growing amount depends primarily on temperature, is lower than 1350 ℃ can produce hardly, is higher than 1500 ℃ of a large amount of generations, because the clinkering zone flame temperature is up to 1800 ℃ in the rotary kiln, airborne N
2And O
2Rapid reaction, thermal NO x generates in a large number.
2, " fuel type " NOx:
Manufacture of cement fuel is mainly coal, and fuel produces " fuel type " NOx in burning.
3, " Quick-type " NOx:
The NOx that the N of air and the group of the ionic hydrocarbon in the fuel produce such as reactions such as CH when burning, this NOx is inappreciable in the manufacture of cement.
Below in conjunction with Fig. 1 in this Figure of description prior art is analyzed.
As shown in Figure 1, cement clinker production line comprises cyclone cylinder 1, decomposing furnace 2, burner 3, Uptake flue at kiln end 4, kiln tail smoke-box 5 rotary kilns 6, tertiary-air pipe 14, cooler 17.
In the combustion gas, the NOx emission concentration is 400～900ppm(500～1100mg/Nm
3);
In the decomposing furnace 2, temperature is 800～1200 ℃, mainly produces fuel type NOx;
In the kiln tail smoke-box 5, the concentration of NOx is 800～1500ppm(1000～1900mg/Nm
3);
In the rotary kiln 6, temperature mainly produces heating power type and fuel type NOx up to more than 1600 ℃;
Cooler 17 is discharged hot exhausting (being coal mill dry wind) and the lingering remnants of past customs.
Three, the basic skills of NOx improvement:
Because burning is the major cause that NOx produces, so, the basic skills of its improvement be formulated according to the characteristics of combustion processes.
Put it briefly, but the three kinds of methods of processing after the improvement of the processing before the improvement method divided combustion of NOx, combustion system and the burning.
1, burning pre-treatment: the burning pre-treatment mainly is the denitrogenation of carrying out fuel;
What 2, the improvement of combustion system was at present practical is to adopt the low nitrogen burning technology such as low nitrogen oxide burner, fractional combustion;
3, the processing after the burning refers to that mainly gas denitrifying technology mainly comprises selective non-catalytic reduction technology (SNCR) and SCR technology (SCR) etc.
Characteristics and advantages according to cement industry, take the low nitrogen burning technology, start with from cement firing system process characteristic, generation at source control NOx, reach the purpose that NOx reduces discharging, relatively to gear to actual circumstances at present, both economical effectively, the technical measures of energy-conserving and environment-protective, have higher feasibility and great research and promotion and implementation are worth.
Four, fractional combustion denitride technology:
1, grading combustion technology principle:
The ultimate principle of fractional combustion denitrogenation is to set up the reduction combustion zone between smoke-box and decomposing furnace, and former decomposing furnace is uniform in this zone with the part of coal, makes its anoxycausis in order to produce CO, CH
4, H
2, the reductive agent such as HCN and fixed carbon.NOx in these reductive agents and the kiln exit gas reacts, and NOx is reduced into N
2Etc. free of contamination rare gas element.In addition, coal dust burns under anoxia condition and has also suppressed self fuel type NOx generation, thereby realizes that the NOx in the cement production process reduces discharging.Its principal reaction is as follows:
2CO+2NO→N
2+2CO
2
2H
2+2NO→N
2+2H
2O
2NHi+2NO→N
2+…
Grading combustion technology mainly contains two types of Researched of Air Staging Combustion Burning Pulverized Coal and fuel stagings, and we mainly study and what adopt is the fuel-staged combustion technology at present.
2, the problem of grading combustion technology existence of the prior art:
According to the application experience of grading combustion technology on 10000 tons of lines of domestic daily output of having gone into operation, and the assembly line operation status that the domestic application grading combustion technology is transformed understands, and we sum up in the past that grading combustion technology has following problem and shortage:
(1), the reduction zone skinning is serious, affects the normal steady running of system, is difficult to safeguard produce, cause and can not use this technology in the actual production or remove this technological facilities;
(2), to former, fuel quality is strict, the hard coal effect that particularly volatile matter is lower is relatively poor;
(3), technological operation is required harshness, needs control kiln tail O
2Content below 2%, be difficult in the actually operating accomplish;
(4), need to increase independent hello coal metering system and larger hello coal power;
(5), denitration efficiency is unstable, is difficult to reach 30%;
(6), denitration retrofit work amount is large, the time is long, investment is large, running cost improves.
Summary of the invention
The invention provides a kind of new dry process rotary kiln clinker production line, its objective is the operating mass that improves denitration effect and system.
To achieve these goals, the technical scheme taked of the present invention is:
New dry process rotary kiln clinker production line provided by the present invention comprises cyclone cylinder, decomposing furnace, burner, tertiary-air pipe, Uptake flue at kiln end, kiln tail smoke-box and rotary kiln;
The pulverized coal channel that leads to the kiln tail is divided into two-way by the first pulverized coal distributor with coal dust, and wherein, a-road-through is toward the cylinder on described decomposing furnace top, and another road leads to the cone of described decomposing furnace bottom;
Lead to the pulverized coal channel of the cylinder on described decomposing furnace top, again coal dust is divided into two-way by the second pulverized coal distributor, enter symmetrically in the cylinder on described decomposing furnace top;
Lead to the pulverized coal channel of the cone of described decomposing furnace bottom, again coal dust is divided into two-way by the second pulverized coal distributor, enter symmetrically in the cone of described decomposing furnace bottom.
Described decomposing furnace is provided with four burners altogether, comprises two top burner and two lower burner;
Described top burner becomes 20 °～50 ° angle to enter decomposing furnace with horizontal plane, and two top burner are arranged symmetrically with in the level cross-sectionn of described decomposing furnace;
Described lower burner horizontal tangential enters decomposing furnace, and two lower burner are arranged symmetrically with in the level cross-sectionn of described decomposing furnace.
Vertical range between described top burner and the lower burner is 3～6m.
The horizontal cross sectional geometry of described Uptake flue at kiln end is square, and the height of Uptake flue at kiln end is 1200～3000mm.
Described square size dimension is 2000mm.
The feed opening of the C4 cyclone cylinder in the described cyclone cylinder is arranged on the bottom of described decomposing furnace.
Being shaped as of the ingress of described tertiary-air pipe is square, and it is of a size of 2380 * 3080mm.
In described junction, tapering at Uptake flue at kiln end and decomposing furnace the lifting boss is set.
Described lifting boss and inside, decomposing furnace cone junction are the cancave cambered surface of R200～R500mm.
In order to realize the goal of the invention identical with technique scheme, the denitrating technique method that the present invention also provides above-mentioned new dry process rotary kiln clinker production line to adopt, its technical scheme is:
The coal dust amount that enters the cylinder on described decomposing furnace top accounts for 35～45% of the total coal dust amount of kiln tail; The coal dust that will enter the cylinder on decomposing furnace top by the second pulverized coal distributor again is divided into two-way, and its coal dust amount respectively accounts for 50%, and symmetry enters decomposing furnace;
The coal dust amount that enters the cone of described decomposing furnace bottom accounts for 55～65% of the total coal dust amount of kiln tail; The coal dust that will enter the cone of decomposing furnace bottom by the second pulverized coal distributor again is divided into its coal dust amount of two-way and respectively accounts for 50%, and symmetry enters decomposing furnace.
The wind speed of described tertiary-air pipe ingress is 18～22m/s.
The present invention adopts technique scheme, reduces the also interior thermal NO x that produces of reduction kiln, suppresses the generation of fuel type NOx, can be from the effectively generation of reduction NOx on the source; Non-secondary pollution does not have pollutent or by product to generate; The normal production run of production line and cement clinker output and quality are had no adverse effect; Need not to consume the goods and materials such as ammoniacal liquor or urea, do not increase the production run cost; After the technological transformation, make operating parameter optimized, system's operating mass and stability promote, and certain energy-saving effect is arranged.
Description of drawings
The below makes brief description to the expressed content of each width of cloth accompanying drawing of this specification sheets and the mark among the figure:
Fig. 1 is the described cement clinker line of this specification sheets background technology part and the generation position of NOx thereof, the synoptic diagram of generation;
Fig. 2 is the schematic diagram of decomposing furnace staged combustion systems of the present invention;
Fig. 3 is the schematic appearance of staged combustion systems of the present invention;
Fig. 4 is the A-A diagrammatic cross-section among Fig. 3;
Fig. 5 is the K-K diagrammatic cross-section among Fig. 4;
Fig. 6 is the process flow sheet of staged combustion systems of the present invention;
Fig. 7 is the structural representation of burner of decomposition furnace among the present invention;
Fig. 8 is the structural representation of pulverized coal distributor among the present invention.
Be labeled as among the figure:
1, cyclone cylinder, 2, decomposing furnace, 3, burner, 4, Uptake flue at kiln end, 5, kiln tail smoke-box, 6, rotary kiln, the 7, first pulverized coal distributor, the 8, second pulverized coal distributor, 9, divider entrance, 10, coal dust sub-material variable valve, 11, export distributor, 12, top burner, 13, lower burner, 14, tertiary-air pipe, 15, the lifting boss, 16, pulverized coal channel, 17, cooler, 18, the PH boiler, 19, gate valve, 20, tensimeter, the 21, second pulverized coal distributor.
Embodiment
The below contrasts accompanying drawing, and the description by to embodiment is described in further detail the specific embodiment of the present invention, to help those skilled in the art inventive concept of the present invention, technical scheme is had more complete, accurate and deep understanding.
The of the present invention structure expressed such as Fig. 1 is new dry process rotary kiln clinker production line and denitrating technique method thereof, comprises cyclone cylinder 1, decomposing furnace 2, burner 3, tertiary-air pipe 14, Uptake flue at kiln end 4, kiln tail smoke-box 5 and rotary kiln 6.The present invention is and the diverse NOx emission-reduction technology of the fractional combustion of prior art.
As shown in Figure 6, described air duct 1 comprises two row: C1A, C2A, C3A, C4A, C5A from top to bottom; C1B, C2B, C3B, C4B, C5B.
Also expression among Fig. 6: the new dry process rotary kiln clinker production line also is provided with PH boiler 18, and namely kiln tail waste heat boiler is used for the cogeneration of kiln tail.
The present invention responds national environmental protection and reduces discharging policy, and exploitation and the application of low nitrogen burning technology are furtherd investigate, and decomposing furnace is implemented the grading combustion technology transformation, and the NOx emission reduction effect is obvious after transforming.The present invention is by the research to the burning form of coal dust in the decomposing furnace, internal temperature field, air motion situation etc., move difficult point in conjunction with the process characteristic of firing system and the enforcement of grading combustion technology, by research and the comparison to low nitrogen burning technology and gas denitrifying technology, and combine with the process characteristic of cement clinker production line, obtain desirable effect.
In order to solve the problem that prior art exists and to overcome its defective, realize improving the goal of the invention of the operating mass of denitration effect and system, the technical scheme that the present invention takes is:
As shown in Figure 6, new dry process rotary kiln clinker production line provided by the present invention, the pulverized coal channel that leads to the kiln tail is divided into two-way by the first pulverized coal distributor 7 with coal dust, wherein, a-road-through is toward the cylinder on described decomposing furnace 2 tops, and another road leads to the cone of described decomposing furnace 2 bottoms;
Lead to the pulverized coal channel of the cylinder on described decomposing furnace 2 tops, again coal dust is divided into two-way by the second pulverized coal distributor 21, enter symmetrically in the cylinder on described decomposing furnace 2 tops;
Lead to the pulverized coal channel of the cone of described decomposing furnace 2 bottoms, again coal dust is divided into two-way by the second pulverized coal distributor 8, enter symmetrically in the cone of described decomposing furnace 2 bottoms.
Described decomposing furnace 2 is provided with four burners altogether, comprises two top burner 12 and two lower burner 13;
Described top burner 12 becomes 20 °～50 ° angle to enter decomposing furnace 2 with horizontal plane, and two top burner 12 are arranged symmetrically with in the level cross-sectionn of described decomposing furnace 2; For example, top burner 12 becomes 30 ° angle to enter decomposing furnace 2 with horizontal plane;
Described lower burner 13 horizontal tangentials enter decomposing furnace 2, and two lower burner 13 are arranged symmetrically with in the level cross-sectionn of described decomposing furnace 2.
That is to say that each pulverized coal channel enters the position of decomposing furnace 2, be equipped with a burner.
Vertical range between described top burner 12 and the lower burner 13 is 3～6m.For example generally adopt 4 m.
The structure of top burner 12 and lower burner 13 as shown in Figure 7.
Adopt the technical scheme of decomposing furnace reduction zone among the present invention:
The establishment of decomposing furnace reduction zone is most important.The present invention is by the redesign to burner of decomposition furnace 3 positions, kiln tail coal powder is divided into four points, the two-layer decomposing furnace 2 that enters up and down, determine to enter speed, position, angle, cutting angle of the coal dust of decomposing furnace 2 etc., directly affect the burning form of coal dust in decomposing furnace 2 and the formation quality of reduction zone.The reduction zone mainly is the coal dust that sprays into by two burners of lower floor (being lower burner 13), and burning produces under anoxia condition, thereby play the NOx that produces in the kiln is reduced the effect of denitration.
Tapering at decomposing furnace 2 forms the denitrogenation reduction zone that does not produce skinning, and main the employing carried out shaping to the reduced zone space, and localized hyperthermia and skinning are avoided producing in the position of reasonable Arrangement coal burner (position and angle) and C4 blanking point.
In decomposing furnace taper design denitrogenation reduction zone, increased the combustion space.Guaranteeing the clean-burning while of coal dust, suitably increasing the coal dust feeding ratio in decomposing furnace tapering, guaranteeing the reducing atmosphere that anoxycausis produces, forming the reduction zone in the decomposing furnace tapering, a large amount of NOx in the reduction kiln exit gas produces good denitration efficiency;
Correspondingly, the conveying of coal dust and allocative decision:
Coal powder conveying system to the kiln tail redesigns, and by first pulverized coal distributor coal dust is divided into two-way to the pulverized coal channel of kiln tail, and one the tunnel enters the cylinder (top) of decomposing furnace 2, and one the tunnel enters the cone (bottom) of decomposing furnace;
Because burner of decomposition furnace has four, and the coal amount of the feeding design of two burners in top and two burners in bottom is different, therefore, caliber and wind speed to pulverized coal channel have carried out particular design, satisfy the requirement (top 35～45% of burner injecting coal quantity by the design of pulverized coal channel, bottom 55～65%), by the suitable adjusting of pulverized coal distributor, realize optimal running effect again.
Its technical scheme is:
As shown in Figure 8, in the first pulverized coal distributor 7, the second pulverized coal distributor 8 and the second pulverized coal distributor 21, coal dust sub-material variable valve 10 is set, described coal dust sub-material variable valve 10 is arranged between divider entrance 9 and the export distributor 11, is used for carrying out the distribution adjusting of coal dust operational throughput;
As shown in Figure 6, at pulverized coal channel 16 gate valve 19 is set, is used for carrying out the distribution adjusting of coal dust operational throughput; At pulverized coal channel 16 tensimeter 20 is set also, is used for the transfer pressure of monitoring pulverized coal channel 16.
The commutation technique scheme of kiln exit gas:
Develop decomposing furnace fuel-staged combustion technology stably manufactured, greater efficiency, its phenomenons such as skinning of whether stablizing, whether produce directly affect the nsp kiln Systems balanth, the present invention mainly comes kiln exit gas is carried out rectification by the transformation to kiln tail smoke-box funnel uptake and lifting boss, thereby comes keeping system stable.
The technical scheme of the transformation of kiln tail smoke-box and funnel uptake:
Such as Fig. 2 and shown in Figure 4, the horizontal cross sectional geometry of described Uptake flue at kiln end 4 is square, and the height of Uptake flue at kiln end 4 is 1200～3000mm.
Air-flow to cement kiln tail funnel uptake 4 carries out rectification, so that the flow field of upstream is more smooth and easy; The flue gas that namely kiln tail smoke-box 5 is entered decomposing furnace 2 carries out rectification, is transformed into the funnel uptake shape square; Simultaneously, with the straight section prolongation of funnel uptake, it is stable to make the interior flue gas of kiln enter the stove flow field, and reduction enters the stove wind speed.
Described square size dimension is about 1200～3000mm.
The adjustment technology scheme of C4 cyclone cylinder blanking point position:
As shown in Figure 2, the feed opening of the C4 cyclone cylinder in the described cyclone cylinder 1 is arranged on the bottom of described decomposing furnace 2.
Position and running condition according to former firing system C4 cyclone cylinder blanking point, Thermal load of cross-section data calculated in conjunction with the tapering of transforming rear decomposing furnace 2, adjust the position of C4 cyclone cylinder blanking point, generally the blanking of C4 cyclone cylinder is displaced downwardly to decomposing furnace cylinder bottom and top position, tapering, raw material are glided along the tapering of decomposing furnace 2 is inner, raw material absorb heat in the tapering, avoid the generation of decomposing furnace 2 tapering high temperature skinnings.
The technical scheme of decomposing furnace tapering lifting boss:
As shown in Figures 2 and 3, in described junction, tapering at Uptake flue at kiln end 4 and decomposing furnace 2 lifting boss 15 is set.
At Uptake flue at kiln end 4 and decomposing furnace 2 tapering intersections lifting boss 15 is set, can disperse better the raw material that fall and kick up, prevent that raw material from collapsing material directly into rotary kiln 6, the material phenomenon of avoiding collapsing occurs, be easy to simultaneously mixing of raw material and air-flow, avoid producing the localized hyperthermia district;
The structure of described lifting boss 15 is: described lifting boss 15 is the cancave cambered surface of R200～R500mm with inside, decomposing furnace 2 cone junctions.For example, adopt the cancave cambered surface of R300mm.
In order to realize the goal of the invention identical with technique scheme, the denitrating technique method that the present invention also provides above-mentioned new dry process rotary kiln clinker production line to adopt, its technical scheme is:
35～45%(that the coal dust amount that enters the cylinder on described decomposing furnace 2 tops accounts for the total coal dust amount of kiln tail for example can get 40%); The coal dust that will enter the cylinder on decomposing furnace 2 tops by the second pulverized coal distributor 21 again is divided into two-way, and its coal dust amount respectively accounts for 50%, and symmetry enters decomposing furnace 2;
55～65%(that the coal dust amount that enters the cone of described decomposing furnace 2 bottoms accounts for the total coal dust amount of kiln tail for example can get 60%; The coal dust that will enter the cone of decomposing furnace 2 bottoms by the second pulverized coal distributor 8 again is divided into its coal dust amount of two-way and respectively accounts for 50%, and symmetry enters decomposing furnace 2.
The coal dust amount that enters decomposing furnace cylinder (top) accounts for about 40% of the total coal dust amount of kiln tail, the coal dust that simultaneously, will enter decomposing furnace cylinder (top) by second pulverized coal distributor again is divided into two-way (respectively accounting for 50%) symmetry and enters decomposing furnace cylinder (top).
Equally, the coal dust amount that enters decomposing furnace cone (bottom) accounts for about 60% of the total coal dust amount of kiln tail, the coal dust that simultaneously, will enter decomposing furnace cone (bottom) by second pulverized coal distributor again is divided into two-way (respectively accounting for 50%) symmetry and enters decomposing furnace cylinder (bottom).
The adjustment technology scheme of tertiary-air pipe entrance:
The wind speed of described tertiary-air pipe 14 ingress is 18～22m/s.
Enter the needs of stove speed and Flow Field Distribution according to the original system tertiary air, adjust tertiary air inlet area size and enter the stove wind speed;
Fractional combustion generally can reduce the kiln ventilation amount after transforming, and tertiary air quantity increases relatively, in order to guarantee the tertiary air inlet velocity about 18～22m/s, need to redesign tertiary air entrance size
As shown in Figure 5, being shaped as of the entrance of described tertiary-air pipe 14 is square, its be of a size of among 2380 * 3080mm(Fig. 5 wide * height).
The present invention is directed to the present situation of prior art, take full advantage of the process characteristic of cement firing system, to feeding decomposing furnace fuel spray into the position and the burning form redesigns, guarantee that fuel produces reducing atmosphere in decomposing furnace tapering anoxycausis, the thermal NO x that produces in the reduction kiln reaches the denitration purpose about 30%.Simultaneously, generation for fear of unfavorable phenomenons such as the material that collapses, high temperature skinning, kiln tail smoke-box and funnel uptake, C4 blanking point, tertiary air blast inlet etc. are carried out transformation and optimization, solve the problem that existed during grading combustion technology was used in the past, guarantee that native system reaches preferably denitration effect and operating performance.
Technical characterstic of the present invention is:
On operating, suitably reduce kiln ventilation and feed the coal amount, increase tertiary air quantity and Coaling of Decomposing Furnace, excess air coefficient in the reduce kiln, the growing amount of minimizing NOx;
Reduce the high-temperature blower rotating speed, minimizing system wind can reduce grog and burn till hear rate when guaranteeing denitration efficiency as far as possible, and the simultaneity factor resistance decreases;
Create brand-new kiln tail burner fractional combustion arrangement form, effectively made up the denitration reduction zone in decomposing furnace inside, had significant denitration effect;
Distribute by the design of kiln tail burner being fed the coal amount, and the adjustment optimization of C4 blanking point, rationally control decomposing furnace section thermal load, avoided the generation of reduction zone Coating clogging phenomenon;
The flue gas that the kiln tail is entered decomposing furnace has carried out rectification, is provided with decomposing furnace end opening lifting boss, has strengthened the Combination of flue gas and material and coal dust, has avoided the generation of material phenomenon of collapsing, and has stablized kiln ventilation;
By the design that rearranges of kiln tail burner, increased the combustion space of coal dust, when setting up the denitration reduction zone, guaranteed the perfect combustion of coal dust, strengthened the adaptability to fuel;
Fractional combustion is combined with operation optimization, greatly promoted the operating mass of denitration effect and system.
Transformation to grading combustion technology has following technical superiority:
1, technological operation combines, and reduces and the interior thermal NO x that produces of reduction kiln, suppresses the generation of fuel type NOx, can effectively reduce from the source generation of NOx;
2, non-secondary pollution does not have pollutent or by product to generate;
3, the normal production run of production line and cement clinker quality are had no adverse effect;
4, need not to consume the goods and materials such as ammoniacal liquor or urea, do not increase the production run cost;
5, after the technological transformation, make operating parameter optimized, system's operating mass and stability promote, and certain energy-saving effect is arranged.
After technical scheme of the present invention was implemented, final comprehensive denitration efficiency was about 30% so that preheater outlet NOx concentration is reduced to 350～500ppm, and simultaneously, system does not produce the problems such as skinning, can stablize and put into operation.
The above has carried out exemplary description to the present invention by reference to the accompanying drawings; obviously specific implementation of the present invention is not subjected to the restriction of aforesaid way; as long as adopted the improvement of the various unsubstantialities that method of the present invention design and technical scheme carry out; or without improving design of the present invention and technical scheme are directly applied to other occasion, all within protection scope of the present invention.
Claims (10)
1. a new dry process rotary kiln clinker production line comprises cyclone cylinder (1), decomposing furnace (2), burner (3), tertiary-air pipe (14), Uptake flue at kiln end (4), kiln tail smoke-box (5) and rotary kiln (6), it is characterized in that:
The pulverized coal channel that leads to the kiln tail is divided into two-way by the first pulverized coal distributor (7) with coal dust, and wherein, a-road-through is toward the cylinder on described decomposing furnace (2) top, and another road leads to the cone of described decomposing furnace (2) bottom;
Lead to the pulverized coal channel of the cylinder on described decomposing furnace (2) top, again coal dust is divided into two-way by the second pulverized coal distributor (21), enter symmetrically in the cylinder on described decomposing furnace (2) top;
Lead to the pulverized coal channel of the cone of described decomposing furnace (2) bottom, again coal dust is divided into two-way by the second pulverized coal distributor (8), enter symmetrically in the cone of described decomposing furnace (2) bottom.
2. according to new dry process rotary kiln clinker production line claimed in claim 1, it is characterized in that:
Described decomposing furnace (2) is provided with four burners altogether, comprises two top burner (12) and two lower burner (13);
Described top burner (12) becomes 20 °～50 ° angle to enter decomposing furnace (2) with horizontal plane, and two top burner (12) are arranged symmetrically with in the level cross-sectionn of described decomposing furnace (2);
Described lower burner (13) horizontal tangential enters decomposing furnace (2), and two lower burner (13) are arranged symmetrically with in the level cross-sectionn of described decomposing furnace (2).
3. according to new dry process rotary kiln clinker production line claimed in claim 2, it is characterized in that: the vertical range between described top burner (12) and the lower burner (13) is 3～6m.
4. according to new dry process rotary kiln clinker production line claimed in claim 1, it is characterized in that: the horizontal cross sectional geometry of described Uptake flue at kiln end (4) is square, and the height of Uptake flue at kiln end (4) is 1200～3000mm.
5. according to new dry process rotary kiln clinker production line claimed in claim 1, it is characterized in that: the feed opening of the C4 cyclone cylinder in the described cyclone cylinder (1) is arranged on the bottom of described decomposing furnace (2).
6. according to new dry process rotary kiln clinker production line claimed in claim 1, it is characterized in that: being shaped as of the ingress of described tertiary-air pipe (14) is square.
7. according to new dry process rotary kiln clinker production line claimed in claim 1, it is characterized in that: in described junction, tapering at Uptake flue at kiln end (4) and decomposing furnace (2) lifting boss (15) is set.
8. according to new dry process rotary kiln clinker production line claimed in claim 7, it is characterized in that: described lifting boss (15) is the cancave cambered surface of R200～R500mm with decomposing furnace (2) cone internal connection.
9. according to the denitrating technique method of each described new dry process rotary kiln clinker production line in the claim 1 to 8, it is characterized in that:
The coal dust amount that enters the cylinder on described decomposing furnace (2) top accounts for 35～45% of the total coal dust amount of kiln tail; The coal dust that will enter the cylinder on decomposing furnace (2) top by the second pulverized coal distributor (21) again is divided into two-way, and its coal dust amount respectively accounts for 50%, and symmetry enters decomposing furnace (2);
The coal dust amount that enters the cone of described decomposing furnace (2) bottom accounts for 55～65 of the total coal dust amount of kiln tail; The coal dust that will enter the cone of decomposing furnace (2) bottom by the second pulverized coal distributor (8) again is divided into its coal dust amount of two-way and respectively accounts for 50%, and symmetry enters decomposing furnace (2).
10. according to new dry process rotary kiln clinker production line claimed in claim 9, it is characterized in that: the wind speed of described tertiary-air pipe (14) ingress is 18～22m/s.
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