燃煤鍋爐的燃燒進(jìn)程控制-畢業(yè)設(shè)計(jì)外文翻譯

1、Controlling the Furnace Process in Coal-Fired BoilersThe unstable trends that exist in the market of fuel supplied to thermal power plants and the situations in which the parameters of their operation need to be changed (or preserved), as well as the tendency toward the economical and environmental

2、requirements placed on them becoming more stringent, are factors that make the problem of controlling the combustion and heat transfer processes in furnace devices very urgent. The solution to this problem has two aspects. The first involves development of a combustion technology and,accordingly, th

3、e design of a furnace device when new installations are designed. The second involves modernization of already existing equipment. In both cases,the technical solutions being adopted must be properly substantiated with the use of both experimental and calculationstudies.The experience Central Boiler

4、-Turbine Institute Research and Production Association (TsKTI) and ZiO specialists gained from operation of boilers and experimental investigations they carried out on models allowed them to propose several new designs of multifuel and maneuverablein other words, controllable furnace devices that ha

5、d been put in operation at power stations for several years. Along with this, an approximate zero-one-dimensional, zonewise calculation model of the furnace process in boilers had been developed at the TsKTI, which allowed TsKTI specialists to carry out engineering calculations of the main parameter

6、s of this process and calculate studies of furnaces employing different technologies of firing and combustion modes .Naturally, furnace process adjustment methods like changing the air excess factor, stack gas recirculation fraction, and distribution of fuel and air among the tiers of burners, as we

7、ll as other operations written in the boiler operational chart, are used during boiler operation.However, the effect they have on the process is limited in nature. On the other hand, control of the furnace process in a boiler implies the possibility of making substantial changes in the conditions un

8、der which the combustion and heat transfer proceed in order to considerably expand the range of loads, minimize heat losses, reduce the extent to which the furnace is contaminated with slag, decrease the emissions of harmful substances, and shift to another fuel. Such a control can be obtained by ma

9、king use of the following three main factors:(i) the flows of oxidizer and gases being set to move in the flame in a desired aerodynamic manner;(ii) the method used to supply fuel into the furnace and the place at which it is admitted1thereto;(iii) the fineness to which the fuel is milled.The latter

10、 case implies that a flame-bed method is used along with the flame method for combusting fuel.The bed combustion method can be implemented in three design versions: mechanical grates with a dense bed, fluidized-bed furnaces, and spouted-bed furnaces.As will be shown below, the first factor can be ma

11、de to work by setting up bulky vortices transferring large volumes of air and combustion products across and along the furnace device. If fuel is fired in a flame, the optimal method of feeding it to the furnace is to admit it to the zones near the centers of circulating vortices, a situation especi

12、ally typical of highly intense furnace devices. The combustion process in these zones features a low air excess factor ( < 1) and a long local time for which the components dwell in them, factors that help make the combustion process more stable and reduce the emission of nitrogen oxides .Also im

13、portant for the control of a furnace process when solid fuel is fired is the fineness to which it is milled; if we wish to minimize incomplete combustion, the degree to which fuel is milled should be harmonized with the location at which the fuel is admitted into the furnace and the method for suppl

14、ying it there, for the occurrence of unburned carbon may be due not only to incomplete combustion of large-size fuel fractions, but also due to fine ones failing to ignite (especially when the content of volatiles Vdaf < 20%).Owing to the possibility of pictorially demonstrating the motion of flo

15、ws, furnace aerodynamics is attracting a great deal of attention of researchers and designers who develop and improve furnace devices. At the same time, furnace aerodynamics lies at the heart of mixing (mass transfer), a process the quantitative parameters of which can be estimated only indirectly o

16、r by special measurements. The quality with which components are mixed in the furnace chamber proper depends on the number, layout, and momenta of the jets flowing out from individual burners or nozzles, as well as on their interaction with the flow of flue gases, with one another, or with the wall.

17、It was suggested that the gas-jet throw distance be used as a parameter determining the degree to which fuel is mixed with air in the gas burner channel. Such an approach to estimating how efficient the mixing is may to a certain degree be used in analyzing the furnace as a mixing apparatus. Obvious

18、ly, the greater the jet length (and its momentum), the longer the time during which the velocity gradient it creates in the furnace will persist there, a parameter that determines how completely the flows are mixed in it. Note that the higher the degree to which a jet is turbulized at the outlet fro

19、m a nozzle or burner, the shorter the distance which it covers, and, accordingly, the less completely the components are mixed in the furnace volume. Once through burners have advantages over swirl ones in this respect.2It is was proposed that the extent to which once through jets are mixed as they

20、penetratewith velocity w2 and density 2 into a transverse (drift) flow moving with velocity w1 andhaving density 1 be correlated with the relative jet throw distance followingthe wayWhere ks is a proportionality factor that depends on the pitch between the jet1.51.8).The results ofan experimental in

21、vestigation inwhich the mixingof gas with air in aburner and then in a furnace was studied using the incompleteness of mixing as a parameterare reported in 5.A round once through jet is intensively mixed with the surrounding medium in a furnacewithin its initial section, where the flow velocity at t

22、he jet axis is still equal to the velocity w2at the nozzle orificeof radius r0.The velocityofthe jet blowninto the furnace drops veryrapidly beyond theconfines ofthe initial section, and theaxis ithas in the case ofwall-mounted burners bends toward the outlet from the furnace.One may consider that t

23、here are three theoretical models for analyzing the mixing of jetswith flowrate G2 that enter into a stream withflowrate G1. The firstmodel is for the casewhen jets flow into a free space (G1= 0),the second model is for the case when jets flowinto a transverse (drift) current with flowrate G1G2， and

24、 the third model is for the casewhen jets flow into a drift stream with flowrate G1<G2. The second model represents mixingin the channel of a gas burner, and the third model represents mixing in a furnace chamber.We assume that the mixing pattern we have in a furnace is closer to the first model

25、than it is tothe second one, since 0 <G1/G2< 1, and we will assume that the throw distance h of the jetbeing drifted is equal to the length S0 of the free jet s initial section. The ejection ability ofthe jet being drifted then remains the same as that of the free jet, and the length of theini

26、tialsection can be determined using the well-known empirical formula of G.N. Abramovich6 ： S0= 0.67r0/a, (2)where a is the jet structure factor and r0 is the nozzle radius.At a = 0.07, the length of the round jet s initial section is equal to 10 r0 and the radius tjet has at the transition section (

27、at the end of the initial section) is equal to 3.3 r0. The mass flowrate in the jet is doubled in this case. The corresponding minimum furnace cross-sectional area Ff for a round once through burner with the outlet cross-sectional area Fb will then be equal to and the ratio Ff/Fb 20This. value is cl

28、ose to theactual values found in furnaces equipped with once through burners. In furnaces equipped with swirl burners, a= 0.14 and Ff/Fb 10. In both cases, the interval between the burners is equal to the jet diameter in the transition section d tr , which differs little from the value that has been

29、 established in practice and recommended in 7.The method traditionally used to control the furnace process in large boilers consists of3equipping them with a large number of burners arranged in several tiers. Obviously, if the distance between the tiers is relatively small, operations on disconnecti

30、ng or connecting them affect the entire process only slightly. A furnace design employing large flat-flame burners equipped with means for controlling the flame core position using the aerodynamic principle is a step forward. Additional possibilities for controlling the process in TPE-214 and TPE-21

31、5 boilers with a steam output of 670 t/h were obtained through the use of flat-flame burners arranged in two tiers with a large distance between the tiers; this made it possible not only to raise or lower the flame, but also to concentrate or disperse the release of heat in it 1. A verytangible effe

32、ct was obtained from installing multifuel (operating on coal and open-hearth, coke, and natural gases) flat-flame burners in the boilers of cogeneration stations at metallurgical plants in Ukraine and Russia.Unfortunately, we have to state that, even at present, those in charge of selecting the type

33、,quantity, and layout of burners in a furnace sometimes adopt technical solutions that are far from being optimal. This problem should therefore be considered in more detail.If we increase the number of burners nb in a furnace while retaining their total cross-sectional area ( =idem)Fb and the total

34、 flowrate of air through them, their equivalent diameters deq will become smaller, as willthe jet momentums Gbwb, resulting in acorresponding decrease in the jet throw distance hb and the mass they eject. The space with high velocity gradients also becomes smaller, resulting in poorer mixing in the

35、furnace as a whole. This factor becomes especially important when the emissions of NOx and CO aresuppressed rightinside the furnace using staged combustion (at b < 1) underthe conditions of a fortiori nonuniform distribution of fuel among the burners.In 1, a quantitative relationship was establis

36、hed between the parameters characterizing the quality with which once through jets mix with one another as they flow into a limited space with the geometrical parameter of concentration = with nb = idem and Gb = idem. By decreasing this parameter we improve the mass transfer in the furnace; however,

37、 this entails an increase in the flow velocity and the expenditure of energy (pressure drop) in the burners with the same Fb. At the same time, we know from experience and calculations that good mixing in a furnace can be obtained without increasing the head loss if we resort to large long-range jet

38、s. This allows a much less stringent requirement to be placed on the degree of uniformity with which fuel must be distributed among the burners. Moreover, fuel may in this case be fed to the furnace location where it is required from process control considerations.For illustration purposes, we will

39、estimate the effect the number of burners has on the mixing in a furnace at = = idem. schematically shows the plan views of two furnace chambers differing in the number of once through round nozzles (two and four)placed in a tier (on one4side of the furnace). The furnaces have the same total outlet

40、cross-sectional areas of the nozzles ( Fb) and the same jet velocities related to these areas (wb). The well-known swirl furnace of the TsKTI has a design close to the furnace arrangement under consideration. According to the data of 1, the air fraction air that characterizes the mixing and entersth

41、rough once through burners into the furnace volume beneath them can be estimated using the formula air= 1 (3) which has been verified in the range = 0.030.06 for a furnace chamber equipped with two frontal once through burners. Obviously, if we increase the number of burners by a factor of 2, their

42、equivalent diameter, the length of the initial sectionof jets S0 and the areathey serve will reduce by a factor of Then, for example, at = 0.05, the fraction airwill decrease from 0.75 to 0.65. Thus, Eq. (3) may be written in the followingform for approximately assessing the effect of once through b

43、urners on the quality of mixingin a furnace: air =3.15f nb',where is the number of burners (or air nozzles) on one wallwhen they are arranged in one tier both in onesided and opposite manners.The number of burners may be tentatively related to the furnace depth af (at the same=idem) using the ex

44、pression (5)It should be noted that the axes of two large opposite air nozzles ( = 1) an arrangementimplemented in an inverted furnacehad to be inclined downward by more than 50 8.°One well-known example of a furnace device in which once through jets are used to create a large vortex covering a

45、 considerable part of its volume is a furnace with tangentially arranged burners. Such furnaces have received especially wide use in combination with pulverizing fans. However, burners with channels having a small equivalent diameter are frequently used for firing low-calorific brown coals with high

46、 content of moisture. As a result, the jets of air-dust mixture and secondary air that go out from their channels at different velocities(w2/w1 = 2 3) become turbulized and lose the ability to be thrown a long distance; as a consequence, the flame comes closer to the waterwalls and the latter are co

47、ntaminated with slag. One method by which the tangential combustion scheme can be improved consists of organizing the so-called concentric admission of large jets of air-dust mixture and secondary air with thefuel and air nozzles spaced apart from one another over the furnace perimeter, accompanied

48、by intensifying the ventilation of mills 9, 10. Despite the fact that thetemperature level in the flame decreases,the combustion does not become less stable because the fuel mixes with air in a stepwise manner in a horizontal plane.Vortex furnace designs with large vortices the rotation axes of whic

49、h are arranged transversely with respect to the main direction of gas flow have wide possibilitiesin terms of controlling the furnace process. In 1, four furnace schemes with a controllable flame are5described, which employ the principle of large jets colliding with one another; three of these schem

50、es have been implemented. A boiler with a steam capacity of 230 t/h has been retrofitted in accordance with one ofthese schemes (with an inverted furnace) . Tests of this boiler, during which air-dust mixture was fed at a velocity of 25 30 m/s from the boiler front using a highconcentration dust sys

51、tem, showed that the temperature of gases at the outlet from the furnace had a fairly uniform distribution both along the furnace width and depth . A simple method of shifting the flame core over the furnace height was checked during the operation of this boiler, which consisted of changing the rati

52、o of air flowrates through the front and rear nozzles;this allowed a shift to be made from running the furnace in a dry-bottom mode to a slag-tap mode and vice versa. A bottom-blast furnace scheme has received rather wide use in boilers equipped with different types of burners and mills. Boilers wit

53、h steam capacities ranging from 50 to 1650 t/h with such an aerodynamic scheme of furnaces manufactured by ZiO and Sibenergomash have been installed at a few power stations in Russia and abroad . We have to point out that, so far as the efficiency of furnace process control is concerned, a combinati

54、on of the following two aerodynamic schemes is of special interest: the inverted scheme and the bottom-blast one. The flow pattern and a calculation analysis of the furnace process in such a furnace during the combustion of lean coal are presented in 13.Below, two other techniques for controlling th

55、e furnace process are considered. Boilers with flame stoker furnaces have gained acceptance in industrial power engineering, devices that can be regarded to certain degree as controllable ones owing to the presence of two zones in them . Very different kinds of fuel can be jointly combusted in these

56、 furnaces rather easily. An example of calculating such a furnace device is given in 2. As for boilers of larger capacity, work on developing controllable two-zone furnaces is progressing slowly . The development of a furnace device using the so-called VIR technology (the transliterated abbreviation

57、 of the Russian introduction, innovation, and retrofitting) can be considered as holding promise in this respect. Those involved in bringing this technology to the state of industry standard encountered difficulties of an operational nature (the control of the process also presented certain difficulties). In our opinion, these difficulties are due to the fact that the distribution of fuel over fractions can be optimized to a limited extent and that the flow in the main furnac