热风炉控制系统中英文对照外文翻译文献
热风炉中英文说明书
JDK型空气加热器（热风炉）使用说明书Operation Manual of JDKType Air Heater常州市鼎龙环保设备有限公司常州市鼎马干燥机械有限公司Changzhou Dinglong Environmen Protection Equipment Co., Ltd.Changzhou Dingma Drying Machinery Co., Ltd.二00八年敬告用户Notice抽板式链条炉排调风和清灰系统为一体。
Air regulation and dust cleaning system of drawerpanel-type chain grate is a whole.操纵拉杆每2小时往复拉动清灰后复位至需要的风门开度，切记！！！After reciprocating pull and dust cleaning every 2 hours, please reset the control operating rod, and ensure the properopening of the throttle. DO REMEMBER!!!CONTENT1. 概述Summary (1)2. 结构性能简介Brief Introduction of Structural Performance (2)3. 系统图及说明System Drawing and Explanation (3)4. 点火及启动Ignition and Starting (4)5. 烘炉Heat furnace (5)6. 正常运行Normal Operation (6)7. 链条炉排的运行操作和调节Operation and Adjustment of Chain Grate (7)8. 设备保护Protection of the Equipment (12)9. 系统清灰及清渣Dust Cleaning and Slag Removal for the System (13)10. 停炉Shutdown of the Stove (14)11. 维护和保养Maintenance (15)12. 附：沉降室热风炉的清灰 (17)Appendix: dust cleaning of hot blast stove with settling chamber (17)1.概述SummaryJDK系列空气加热器（也称热风炉）是一种以煤为燃料，以空气为介质的新型高效的换热设备，能连续提供恒温、恒压、无尘的干净热空气，广泛应用于纺织漂染、橡胶涂层的热定型；印铁涂料烘房、金属表面除锈处理后的烘干及油漆烘干，造纸工业的烘干，粮食饲料、谷物鱼粉、烟叶茶叶等的烘干；胶合板、石膏板的成型干燥，木材干燥，化工物料、动植物油脂的喷雾干燥以及工业厂房的采暖等等。
温度控制系统论文中英文资料对照外文翻译
温度控制系统论文中英文资料对照外文翻
译
本文将介绍温度控制系统的关键技术，涉及环境温度探测、数
据处理、控制策略等内容。
以下是部分资料的中英文对照外文翻译。
环境温度探测
中文资料
传感器是环境温度控制系统的关键组件之一。
目前市场上主流
的温度传感器有热敏电阻、热电偶、红外线传感器等。
温度控制系
统还需要考虑传感器的输出精度和响应速度等因素。
英文资料
数据处理
中文资料
数据处理是温度控制系统的核心部分。
常用的数据处理方法有滤波、线性化处理、校准等。
数据处理的目的是提高控制精度和稳定性。
英文资料
控制策略
中文资料
控制策略主要包括开环控制和闭环控制。
其中，闭环控制具有更高的控制精度和稳定性，但需要采集反馈信号、进行数据处理等多个步骤。
英文资料
Control strategies mainly include open-loop control and closed-loop control. Among them, closed-loop control has higher control accuracy and stability, but requires multiple steps such as collecting feedback signals and data processing.。
燃煤锅炉 外文翻译 外文文献 英文文献 中英翻译
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 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, the 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 calculation studies.The experience Central Boiler-Turbine Institute Research and Production Association (Ts KTI) and Zi O specialists gained from operation of boilers and experimental investigations they carried out on models allowed them to propose several new designs of multicell and maneuverable—in other words, controllable—furnace devices that had been put in operation at power stations for several years. Along with this, an approximate zero-one-dimensional, zone wise calculation model of the furnace process in boilers had been developed at the Tsk Ti, which allowed Tsk Ti specialists to carry out engineering calculations of the main parameters 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 well 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 under which the combustion and heat transfer proceed in order to considerably expand the range ofloads, 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 making 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 admitted thereto;(iii) the fineness to which the fuel is milled.The latter 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 made to work by setting up bulky vorticisms 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 vorticisms, a situation especially typical of highly intense furnace devices. The combustion process in these zones features a low air excess factor (α< 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 important 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 supplying 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 Daff < 20%).Owing to the possibility of pictorially demonstrating the motion of flows, 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 quantitativeparameters of which can be estimated only indirectly or 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.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. Obviously, 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 turbulence at the outlet from 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.It is was proposed that the extent to which once through jets are mixed as they penetrate with velocity w2 and density ρ2 into a transverse (drift) flow moving with velocity w1 and having density ρ1 be correlated with the relative jet throw distance in the following wayWhere ks is a proportionality factor that depends on the “pitch” between the jet axes (ks= 1.5–1.8).The results of an experimental investigation in which the mixing of gas with air in a burner and then in a furnace was studied using the incompleteness of mixing as a parameter are reported in 5.A round once through jet is intensively mixed with the surrounding medium in a furnace within its initial section, where the flow velocity at the jet axis is still equal to the velocity w2 at the nozzle orifice of radius r0.The velocity of the jet blown into the furnace drops very rapidly beyond the confines of the initial section, and the axis it has in the case of wall-mounted burners bends toward the outlet from the furnace.One may consider that there are three theoretical models for analyzing the mixing of jets with flow rate G2 that enter into a stream with flow rate G1. The firstmodel is for the case when jets flow into a “free” space (G1= 0),the second model is for the case when jets flow into a transverse (drift) current with flow rate G1 G2，and the third model is for the case when jets flow into a drift stream with flow rateG1<G2. The second model represents mixing in 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 than it is to the second one, since 0 <G1/G2< 1, and we will assume that the throw distance h of the jet being drifted is equal to the length S0 of the “free” jet’s initial section. The ejection ability of the jet being drifted then remains the same as that of the “free” jet, and the length of the initial section can be determined using the well-known empirical formula of G.N. Amphibrachic [6] ：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 the jet has at the transition section (at the end of the initial section) is equal to 3.3 r0. The mass flow rate 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 t he ratio Ff/Fb≈20. This value is close to the actual 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 established in practice and recommended in [7].The method traditionally used to control the furnace process in large boilers consists of equipping them with a large number of burners arranged in several tiers. Obviously, if the distance between the tiers is relatively small, operations on disconnecting 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-215 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 orlower the flame, but also to concentrate or disperse the release of heat in it [1]. A very tangible effect was obtained from installing multicell (operating on coal andopen-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, 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 (ΣFb=idem) and the total flow rate of air through them, their equivalent diameters deq will become smaller, as will the jet momentums GB, resulting in a corresponding 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 furnace as a whole. This factor becomes especially important when the emissions of Box and CO are suppressed right inside the furnace using staged combustio n (at αb < 1) under the conditions of a Fortinbras nonuniform distribution of fuel among the burners.In [1], a quantitative relationship was established 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, 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 jets. 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 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 andfour) placed in a tier (on one side of the furnace). The furnaces have the same total outlet cross-sectional areas of the nozzles (ΣF b) 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 βair that characterizes the mixing and enters through once through burners into the furnace volume beneath them can be estimated using the formula βair = 1 – (3) which has been verified in the range = 0.03–0.06 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 equivalent diameter, the length of the initial section of jets S0 and the area they “serve” will reduce by a factor of Then, for example, at = 0.05, the fraction βair will decrease from 0.75 to 0.65. Thus, Eq. (3) may be written in the following form for approximately assessing the effect of once through burners on the quality of mixing in a furnace:βair = 1 – 3.5f nb ' ,where is the number of burners (or air nozzles) on one wall when 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 expression (5)It should be noted that the axes of two large opposite air nozzles ( = 1)—an arrangement implemented in an inverted furnace—had 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 considerable part of its volume is a furnace with tangentially arranged burners. Such furnaces have received especially wide usein combination with pulverizing fans. However, burners with channels having a small equivalent diameter are frequently used for firing low-calorific brown coals with high 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 turbulence and lose the ability to be thrown a long distance; as a consequence, the flame comes closer to the water walls and the latter are contaminated 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 the fueland air nozzles spaced apart from one another over the furnace perimeter, accompanied by intensifying the ventilation of mills [9, 10]. Despite the fact that the temperature 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.V ortex furnace designs with large cortices the rotation axes of which are arranged transversely with respect to the main direction of gas flow have wide possibilities in terms of controlling the furnace process. In [1], four furnace schemes with a controllable flame are described, which employ the principle of large jets colliding with one another; three of these schemes have been implemented. A boiler with a steam capacity of 230 t/h has been retrofitted in accordance with one of these 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 high concentration dust system, 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 ratio of air flow rates through the front and rear nozzles;this allowed a shift to be made from running the furnace in adry-bottom mode to a slag-tap mode and vice Versace. A bottom-blast furnace scheme has received rather wide use in boilers equipped with different types of burners and mills. Boilers with steam capacities ranging from 50 to 1650 t/h with such an aerodynamic scheme of furnaces manufactured by ZiO and Bergomask 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 combination 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 the 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 furnaces rather easily. An example of calculating such a furnacedevice 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 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 furnace volume has a rather sluggish aerodynamic structure. It should also be noted that the device for firing the coarsest fractions of solid fuel in a spouting bed under the cold funnel is far from being technically perfect.Centrifugal dust concentrators have received acceptance for firing high-reactive coals in schemes employing pulverizing fans to optimize the distribution of fuel as to its flow rate and fractions. The design of one such device is schematically shown in [9]. Figure shows a distribution of fuel flow rates among four tiers of burners that is close to the optimum one. This distribution can be controlled if we furnish dust concentrators with a device with variable blades, a solution that has an adequate effect on the furnace process.燃煤锅炉的燃烧进程控制存在于火电厂的市场的燃料供应，某些操作参数需要改变（或保留）的情况下，以及经济和环境方面倾向的要求使他们变得更加严格的不稳定趋势是导致使控制燃烧与传热过程炉设备非常紧迫的主要因素。
控制系统中英文对照
Burner Management System燃烧管理系统CCR:Center control room中控室ER:Engineering room工程师室FRR:Field Rack Room现场仪表机柜室（控制室分站）DCS:Distributed control system集散控制系统ESD:Emergency shut-down system紧急停车系统FAT:Factory Acceptance Test工厂验收测试HMIHuman Machine Interface (operator station)人机接口（操作员站）I/O:Input/Output输入/输出MCCMotor Control Center马达控制中心MMS:Machinery Monitoring System机械监测系统MOV:Motor Operated Valve电动阀P&ID:Piping and Instrument Diagrams管道仪表流程图PFD:Process Flow Diagram工艺流程图PLC:Programmable Logic Controller可编程逻辑控制器PU:Package Unit成套设备SAT:Site Acceptance Test现场认可测试SOE:Sequence Of Events事件序列记录SIL:Safety Integrity Level安全完整性等级SIS:Safety Instrumented System安全仪表系统TMR:Triple Modular Redundant三重模块冗余Quadruple Modular Redundant (dual redundant system) 四重模块冗余（双重冗余系统）UPSUninterruptible Power Supply不间断电源1oo2One out of two, likewise: 2oo32选1，同样地3选2Aabort 中断,停止abnormal 异常abrader 研磨,磨石,研磨工具absence 失去Absence of brush 无(碳)刷Absolute ABS 绝对的Absolute atmosphere ATA 绝对大气压AC Lub oil pump 交流润滑油泵absorptance 吸收比,吸收率acceleration 加速accelerator 加速器accept 接受access 存取accomplish 完成,达到accumulator 蓄电池,累加器Accumulator battery 蓄电池组accuracy 准确,精确acid 酸性,酸的Acid washing 酸洗acknowledge 确认,响应acquisition 发现,取得action 动作Active power 有功功率actuator 执行机构address 地址adequate 适当的，充分的adjust 调整，校正Admission mode 进汽方式Aerial line 天线after 以后air 风，空气Air compressor 空压机Air duct pressure 风管压力Air ejector 抽气器Air exhaust fan 排气扇Air heater 空气加热器Air preheater 空气预热器Air receiver 空气罐Alarm 报警algorithm 算法alphanumeric 字母数字Alternating current 交流电Altitude 高度，海拔Ambient 周围的，环境的Ambient temp 环境温度ammeter 电流表，安培计Ammonia tank 氨水箱Ampere 安培amplifier 放大器Analog 模拟Analog input 模拟输入Analog-to-digital A/D 模拟转换Analysis 分析Angle 角度Angle valve 角伐Angle of lag 滞后角Angle of lead 超前角anthracite 无烟煤Anion 阴离子Anionic exchanger 阴离子交换器Anode 阳极，正极announce 通知，宣布Annual 年的，年报Annual energy output 年发电量anticipate 预期，期望Aph slow motion motor 空预器低速马达Application program 应用程序approach 近似值，接近Arc 电弧，弧光architecture 建筑物结构Area 面积，区域armature 电枢，转子衔铁Arrester 避雷器Ash 灰烬，废墟Ash handling 除灰Ash settling pond 沉渣池Ash slurry pump 灰浆泵assemble 安装，组装Assume 假定,采取,担任Asynchronous motor 异步马达atmosphere 大气，大气压Atomizing 雾化Attempt 企图Attemperater 减温器，调温器Attention 注意Attenuation 衰減,减少,降低Auto reclose 自动重合闸Auto transfer 自动转移Autoformer 自耦变压器Automatic AUTO 自动Automatic voltage regulator 自动调压器Auxiliary AUX 辅助的Auxiliary power 厂用电Available 有效的,可用的Avoid 避免,回避Avometer 万用表,安伏欧表计Axial 轴向的Axis 轴,轴线Axis disp protection 轴向位移，保护Axle 轴，车轴，心捧BBack 背后，反向的Back pressure 背压Back wash 反冲洗Back up 支持，备用Back ward 向后Baffle 隔板Bag filter 除尘布袋Balance 平衡Ball 球Ball valve 球阀Bar 巴，条杆Bar screen material classifier 栅形滤网base 基础、根据Base load 基本负荷Base mode 基本方式Batch processing unit 批处理单元Battery 电池Bearing BRG 轴承before 在…之前bell 铃Belt 带，皮带Bend 挠度，弯曲BLAS 偏置，偏压Binary 二进制，双Black 黑色Black out 大停电，全厂停电blade 叶片Bleed 放气，放水Blocking signal 闭锁信号Blow 吹Blow down 排污Blowlamp 喷灯blue 蓝色Bms watchdog Bms看门狗，bms监视器boiler BLR 锅炉Boiler feedwater pump BFP 锅炉给水泵Boil-off 蒸发汽化bolt 螺栓bore 孔，腔boost BST 增压，提高Boost centrifugal pump BST CEP 凝升泵Boost pump BP 升压泵Boot strap 模拟线路，辅助程序bottom 底部Bowl mill 碗式磨brash 脆性，易脆的bracket 支架，托架，括号breadth 宽度break 断开，断路breaker 断路器，隔离开关Breaker coil 跳闸线路breeze 微风，煤粉Brens-chluss 熄火，燃烧终结bridge 电桥，跨接，桥形网络brigade 班，组，队，大队broadcast 广播brownout 节约用电brush 电刷，刷子Brush rocker 电刷摇环Brown coal 褐煤Buchholtz protecter 瓦斯保护bucket 斗，吊斗Buffer tank 缓冲箱built 建立bulletin 公告，公报bunker 煤仓burner 燃烧器Burner management system 燃烧器管理系统Bus section 母线段busbar 母线Busbar frame 母线支架buscouple 母联button 按钮Bypass/by pass BYP 旁路Bypass valve 旁路阀学习一下，2楼的怎么没有下文了！很吊胃口！我也稍微提供一些，仅供交流参考！也希望2楼的继续有下文阿！仪表功能被测变量温度温差压力或真空压差流量液位或料位变送TT TDT PT PDT FT LT指示TI TDI PI PDI FI LI指示、变送TIT TDIT PIT PDIT FIT LIT指示、调节TIC TDIC PIC PDIC FIC LIC指示、报警TIA TDIA PIA PDIA FIA LIA指示、联锁、报警TISA TDSIA PISA PDSIA FISA LISA指示、积算FIQ指示、自动手动操作TIK TDIK PIK PDIK FIK LIK记录TR TDR PR PDR FR LR记录、调节TRC TDRC PRC PDRC FRC LRC记录、报警TRA TDRA PRA PDRA FRA LRA记录、联锁、报警TRSA TDRSA PRSA PDSRA FRSA LRSA 记录、积算PDRQ FRQ调节TC TDC PC PDC FC LC调节、变送TCT报警TA联锁、报警TSA TDSA PSA PDSA FSA LSA积算、报警FQA火焰报警BA电导率指示CI电导率指示、报警CIA时间或时间程序指示KI时间程序指示控制KIC作者: xqc130******** 时间: 2009-5-4 22:25DCS分散控制系统中英文对照DCS-----------------------------分散控制系统RUNBACK-------------------------自动快速减负荷RUNRP---------------------------强增负荷RUNDOWN-------------------------强减负荷FCB-----------------------------快速甩负荷MFT-----------------------------锅炉主燃料跳闸TSI-----------------------------汽轮机监测系统ETS-----------------------------汽轮机紧急跳机系统TAS-----------------------------汽轮机自启动系统AGC-----------------------------自动发电控制ADS-----------------------------调度自动化系统CCS-----------------------------单元机组协调控制系统FSSS----------------------------锅炉炉膛安全监控系统BMS-----------------------------燃烧管理系统SCS-----------------------------顺序控制系统MCC-----------------------------调节控制系统DAS-----------------------------数椐采集系统DEH-----------------------------数字电液调节系统MEH-----------------------------给水泵汽轮机数字电液调节系统BPS-----------------------------旁路控制系统DIS-----------------------------数字显示站MCS-----------------------------管理指令系统BM------------------------------锅炉主控TM------------------------------汽轮机主控DEB-----------------------------协调控制原理ULD-----------------------------机组负荷指令ABTC----------------------------CCS的主控系统MLS-----------------------------手动负荷设定器BCS-----------------------------燃烧器控制系统PLC-----------------------------可编程控制器UAM-----------------------------自动管理系统MTBF----------------------------平均故障间隔时间MTTR----------------------------平均故障修复时间SPC-----------------------------定值控制系统OPC-----------------------------超数保护控制系统ATC-----------------------------自动汽轮机控制ETS-----------------------------汽轮机危急遮断系统AST-----------------------------自动危急遮断控制IMP------------------------------调节级压力VP------------------------------阀位指令FA------------------------------全周进汽PA------------------------------部分进汽LVDT----------------------------线性位移差动转换器UMS-----------------------------机组主控顺序BMS-----------------------------炉主控顺序BFPT----------------------------给水泵汽轮机PID-----------------------------比例积分微分调节器BATCHDATA-----------------------批数椐节STEPSUBOUTINE-------------------步子程序节FUNCTIONSUBOUTINE—-------------功能子程序节MONITORSUBOUTINE----------------监视子程序节MCR-----------------------------最大连续出力ASP-----------------------------自动停导阀LOB-----------------------------润滑油压低LP------------------------------调速油压低LV------------------------------真空低OS------------------------------超速PU------------------------------发送器RP------------------------------转子位置TB------------------------------轴向位移DPU-----------------------------分散控制单元MIS-----------------------------自动化管理信息系统DEL-----------------------------数据换码符DTE-----------------------------数据终端设备DCE-----------------------------数据通信设备RTU-----------------------------远程终端TXD-----------------------------发送数据RXD-----------------------------接收数据RTS-----------------------------请求发送CTS-----------------------------结束发送DSR-----------------------------数据装置准备好DTR-----------------------------数据终端准备好WORKSTATION---------------------工作站DATAHIGHWAYS--------------------数据高速公路DATANETWORK---------------------数据网络OIS-----------------------------操作员站EWS-----------------------------工程师站MMI-----------------------------人机接口DHC-----------------------------数据高速公路控制器FP------------------------------功能处理器MFC-----------------------------多功能处理器NMRR----------------------------差模抑制比CMRR----------------------------共模抑制比OIU-----------------------------操作员接口MMU-----------------------------端子安装单元CIU-----------------------------计算机接口单元COM-----------------------------控制器模件LMM-----------------------------逻辑主模件BIM-----------------------------总线接口模件AMM-----------------------------模拟主模件DSM-----------------------------数字子模件DLS-----------------------------数字逻辑站ASM-----------------------------模拟子模件DIS-----------------------------数字指示站CTS-----------------------------控制I/O子模件TPL-----------------------------通信回路端子单元TDI/IDO-------------------------数字输入/输出端子单元TAI/TAO-------------------------模拟输入/输出端子单元TLS-----------------------------逻辑站端子单元TCS-----------------------------控制器站端子单元CTM-----------------------------组态调整单元MBD-----------------------------控制板LOG-----------------------------记录器站ENG-----------------------------工程师控制站HSR-----------------------------历史数据存储及检索站OPE-----------------------------操作员/报警控制台CALC----------------------------记算机站TV------------------------------高压主汽阀GV------------------------------高压调节阀RV------------------------------中压主汽阀IV------------------------------中压调节阀PPS-----------------------------汽轮机防进水保护系统AS------------------------------自动同步BOP-----------------------------轴承润滑油泵EOP-----------------------------紧急事故油泵SOB-----------------------------高压备用密封油泵CCBF----------------------------协调控制锅炉跟随方式CCTF----------------------------协调控制汽轮机跟随方式CRT-----------------------------阴极射线管GC------------------------------高压调节阀控制IC------------------------------中压调节阀控制TC------------------------------高压主汽阀控制LDC-----------------------------负荷指令计算机OA------------------------------操作员自动控制PCV-----------------------------压力控制阀门RD------------------------------快速降负荷RSV-----------------------------中压主汽阀TSI-----------------------------汽轮机监控仪表TPC-----------------------------汽轮机压力控制UPS-----------------------------不间断电源HONEYWELL PKS 术语缩写AI Analog Input 模拟量输入AO Analog Output 模拟量输出ACS Automation Control System 自动控制系统CM Control Module 控制模块CNI ControlNet Interface ControlNet接口CPM Control Processor Module 控制处理器模块CR Control Room Area 控制室DI Digital Input 数字量输入DO Digital Output 数字量输出ES Experion Server Experion服务器ESD Emergency Shutdown System 紧急停车系统FB Function Block 功能块FGS-ENG Fire & Gas System Engineering Station 消防和燃气系统工程站FTE Fault Tolerant Ethernet 容错以太网HAI HART Analog Input 带HART协议的模拟量输入IO Input Output 输入输出LAN Local Area Network 局域网MAC Media Access Control 媒体访问控制NIC Network Interface Card 网络接口卡OI Override Interlock 覆写联锁OP Output 输出PCS Process Control System 过程控制系统P-LAN Process LAN 过程局域网P-LAN-A P-LAN A 过程局域网AP-LAN-B P-LAN B 过程局域网BPRN Printer 打印机PRSV Printer Server 打印服务器RCP Redundant Chassis Pair 冗余机架对RM Redundancy Module 冗余模块RTU Remote Terminal Unit 远程终端单元SCM Sequence Control Module 顺控模块SDS Shutdown System 停车系统SI Safety Interlock 安全连锁SP Set Point 设定值STN Experion Station Exrerion站UPS Un-interruptible Power Supply 不间断电源TS Terminal Server 终端服务器MICC（Main Instrument&Control Contractor)主要仪表和控制承包商MAV （Main Automation Vendor）主要自动化供应商MIV（Main Instrument Vendor）主要仪表供应商作者：张强。
热风炉自动控制系统
热风炉自动控制系统孟照崇控制工程2015 153085210040摘要：本论文主要叙述中小型高炉炼铁自动化系统结构、功能及主要系统的自动控制的原理及其实际应用。
着重叙述了热风炉的参数控制过程（热风炉检测仪表及控制系统，热风炉换炉自动控制系统，）和应用。
关键词：热风炉；自动控制；应用Abstract ：This thesis mainly narrates the middle and small scale blast furnace iron-smelting automated system structure, function and mainly control the principle of the system automatically and it is physically applied. Emphasized to describe a process (hot-blast stove detection instrumentation and control system, the hot-blast stove trades the stove automatic control system) that hot-blast stove parameter control and aplly.Keywords: Hot-blast stove； automatic control； application1.前言高炉热风炉是给高炉燃烧提供热风以助燃的设备，是一种储热型热交换器。
国内大部分高炉均采用每座高炉带3至4台热风炉并联轮流送风方式，保证任何瞬时都有一座热风炉给高炉送风，而每座热风炉都按：燃烧-休止-送风-休止-燃烧的顺序循环生产。
当一座或多座热风炉送风时，另外的热风炉处于燃烧或休止状态。
送风中的热风炉温度降低后，处于休止状态的热风炉投入送风，原送风热风炉即停止送风并开始燃烧、蓄热直至温度达到要求后，转入休止状态等待下一次送风。
热电联产中英文对照外文翻译文献
中英文对照外文翻译文献(文档含英文原文和中文翻译)外文文献:The Optimal Operation Criteria for a Gas Turbine Cogeneration System Abstract: The study demonstrated the optimal operation criteria of a gas turbine cogeneration system based on the analytical solution of a linear programming model. The optimal operation criteria gave the combination of equipment to supply electricity and steam with the minimum energy cost using the energy prices and the performance of equipment. By the comparison with a detailed optimization result of an existing cogeneration plant, it was shown that the optimal operation criteria successfully provided a direction for the system operation under the condition where the electric power output of the gas turbine was less than the capacity.Keywords: Gas turbine; Cogeneration; Optimization; Inlet air cooling.1. IntroductionCogeneration, or combined heat and power production, is suitable for industrial users who require large electricity as well as heat, to reduce energy and environmental impact. To maximize cogeneration, the system has to be operated with consideration electricity and heat demands andthe performance of equipment. The optimal operation of cogeneration systems is intricate in many cases, however, due to the following reasons. Firstly, a cogeneration system is a complex of multiple devices which are connected each other by multiple energy paths such as electricity, steam, hot water and chilled water. Secondly, the performance characteristics of equipment will be changed by external factors such as weather conditions.For example, the output and the efficiency of gas turbines depend on the inlet air temperature. Lastly,the optimal solution of operation of cogeneration systems will vary with the ratio of heat demand to electricity demand and prices of gas, oil and electricity.Because of these complexities of cogeneration systems, a number of researchers have optimal solutions of cogeneration systems using mathematical programming or other optimization techniques. Optimization work focusing on gas turbine cogeneration systems are as follows. Yokoyama et al. [1] presented optimal sizing and operational planning of a gas turbine cogeneration system using a combination of non-linear programming and mixed-integer linear programming methods. They showed the minimum annual total cost based on the optimization strategies. A similar technique was used by Beihong andWeiding [2] for optimizing the size of cogeneration plant. A numerical example of a gas turbine cogeneration system in a hospital was given and the minimization of annual total cost was illustrated. Kong et al. [3] analyzed a combined cooling, heating and power plant that consisted of a gas turbine, an absorption chiller and a heat recovery boiler. The energy cost of the system was minimized by a linear programming model and it was revealed that the optimal operational strategies depended on the load conditions as well as on the cost ratio of electricity to gas. Manolas et al. [4] applied a genetic algorithm (GA) for the optimization of an industrial cogeneration system, and examined the parameter setting of the GA on the optimization results. They concluded that the GA was successful and robust in finding the optimal operation of a cogeneration system.As well as the system optimization, the performance improvement of equipment brings energy cost reduction benefits. It is known that the electric power output and the efficiency of gas turbines decrease at high ambient temperatures. Some technical reports [5, 6] show that the electric power output of a gas turbine linearly decreases with the rise of the ambient temperature, and it varies about 5 % to 10 % with a temperature change of 10 ◦C. Therefore, cooling of the turbine inlet air enhances electric output and efficiency. Some studies have examined theperformance of the gas turbine with inlet air cooling as well as the effect of various cooling methods [7, 8, 9].The cooling can be provided without additional fuel consumption by evaporative coolers or by waste heat driven absorption chillers. The optimal operation of the system will be more complex, however, especially in the case of waste heat driven absorption chillers because the usage of the waste heat from the gas turbine has to be optimized by taking into consideration the performance of not only the gas turbine and the absorption chiller but also steam turbines, boilers and so on. The heat and electricity demands as well as the prices of electricity and fuels also influence the optimal operation.The purpose of our study is to provide criteria for optimal operation of gas turbine cogeneration systems including turbine inlet air cooling. The criteria give the minimum energy cost of the cogeneration system. The method is based on linear programming and theKuhn-Tucker conditions to examine the optimal solution, which can be applied to a wide range of cogeneration systems.2. The Criteria for the Optimal Operation of Gas Turbine Cogeneration SystemsThe criteria for the optimal operation of gas turbine cogeneration systems were examined from the Kuhn-Tucker conditions of a linear programming model [10]. A simplified gas turbine cogeneration system was modeled and the region where the optimal solution existed was illustrated on a plane of the Lagrange multipliers.2.1. The Gas Turbine Cogeneration System ModelThe gas turbine cogeneration system was expressed as a mathematical programming model. The system consisted of a gas turbine including an inlet air cooler and a heat recovery steam generator (HRSG), a steam turbine, an absorption chiller, a boiler and the electricity grid. Figure 1 shows the energy flow of the system. Electricity, process steam, and cooling for process or for air-conditioning are typical demands in industry, and they can be provided by multiple suppliers. In the analysis, cooling demands other than for inlet air cooling were not taken into account, and therefore, the absorption chiller would work only to provide inlet air cooling of the gas turbine. The electricity was treated as the electric power in kilowatts, and the steam and the chilled water were treated as the heat flow rates in kilowatts so that the energy balance can be expressed in the same units.Figure 1. The energy flow of the simplified gas turbine cogeneration system with the turbineinlet air cooling.The supplied electric power and heat flow rate of the steam should be greater than or equal to the demands, which can be expressed by Eqs. (1-2).(1)(2)where, xe and xs represent the electric power demand and the heat flow rate of the steam demand. The electric power supply from the grid, the gas turbine and the steam turbine are denoted by xG, xGT and xST, respectively. xB denotes the heat flow rate of steam from the boiler, and xAC denotes the heat flow rate of chilled water from the absorption chiller. The ratio of the heat flow rate of steam from the HRSG to the electric power from the gas turbine is denominated the steam to electricity ratio, and denoted by ρGT. Then, ρGTxGT represents the heat flow rate o f steam from the gas turbine cogeneration. The steam consumption ratios of the steam turbine and the absorption chiller are given as ωST and ωAC, respectively. The former is equivalent to the inverse of the efficiency based on the steam input, and the latter is equivalent to the inverse of the coefficient of performance.The inlet air cooling of the gas turbine enhances the maximum output from the gas turbine. By introducing the capacity of the gas turbine, XGT, the effect of the inlet air cooling was expressed by Eq. (3).(3).It was assumed that the increment of the gas turbine capacity was proportional to the heatflow rate of chilled water supplied to the gas turbine. The proportional constant is denoted byαGT.In addition to the enhancement of the gas turbine capacity, the inlet air cooling improves the electric efficiency of the gas turbine. Provided that the improvement is proportional to the heat flow rate of chilled water to the gas turbine, the fuel consumption of the gas turbine can be expressed as ωGTxGT¡βGTxAC, whereωGT is the fuel consumption ratio without the inlet air cooling and βGT is the improvement factor of the fuel consumption by the inlet air cooling. As the objective of the optimization is the minimization of the energy cost during a certain time period, Δt, the energy cost should be expressed as a function of xG, xGT, xST, xB and xAC. By defining the unit energy prices of the electricity, gas and oil as Pe, Pg and Po, respectively, the energy cost, C, can be given as:(4)where, ωB is the fuel consumpti on ratio of the boiler, which is equivalent to the inverse of the thermal efficiency.All the parameters that represent the characteristics of equipment, such as ωGT, ωST, ωAC, ωB, ρGT, αGT and βGT, were assumed to be constant so that the system could be m odeled by the linear programming. Therefore, the part load characteristics of equipment were linearly approximated.2.2. The Mathematical Formulation and the Optimal Solution From Eqs. (1–4), the optimization problem is formed as follows:(5)(6)(7)(8)where, x = (xG, xGT, xST, xB, xAC). Using the Lagrange multipliers, λ = (λ1, λ2, λ3), theobjectivefunction can be expressed by the Lagrangian, L(x,λ).(9)According to the Kuhn-Tucker conditions, x and λ satisfy the following conditions at the optimal solution.(10)(11)(12)(13)The following inequalities are derived from Eq. (10).(14)(15)(16)(17)(18)Equation (11) means that xi > 0 if the derived expression concerning the supplier i satisfies the equali ty, otherwise, xi = 0. For example, xG has a positive value if λ1 equals PeΔt. If λ1 is less than PeΔt, then xG equals zero.With regard to the constraint g3(x), it is possible to classify the gas turbine operation into two conditions.The first one is the case where the electric power from the gas turbine is less than the capacity,which means xG < XGT + αGTxAC. The second one is the case where the electric power from the gas turbine is at the maximum, which means xGT = XGT + αGTxAC. We denominate the former and the latter conditions the operational conditions I and II, respectively. Due to Eq. (12) of the Kuhn-Tucker condition, λ3 = 0 on the operational condition I, and λ3 > 0 on the operational condition II.2.3. The Optimal Solution where the Electric Power from the Gas Turbine is less than theCapacityOn the operational condition I where xG < XGT + αGTxAC, Eqs. (14–18) can be drawn on the λ1-λ2 plane because λ3 equals zero. The region surrounded by the inequalities gives the feasible solutions, and the output of the supplier i has a positive value, i.e. xi > 0, when the solution exists on the line which represents the supplier i.Figure 2 illustrates eight cases of the feasible solution region appeared on the λ1-λ2 plane. The possible optimal solutions ar e marked as the operation modes “a” to “g”. The mode a appears in the case A, where the grid electricity and the boiler are chosen at the optimal operation. In the mode b,the boiler and the steam turbine satisfy the electric power demand and the heat flow rate of the steam demand. After the case C, the electric power from the gas turbine is positive at the optimal operation.In the case C, the optimal operation is the gas turbine only (mode c), the combination of the gas turbine and the boiler (mode d) or the combination of the gas turbine and the grid electricity (mode e). In this case, the optimal operation will be chosen by the ratio of the heat flow rate of the steam demand to the electric power demand, which will be discussed later. When the line which represents the boiler does not cross the gas turbine line in the first quadrant, which is the case C’, only the modes c and e appear as the possible optimal solutions. The modes f and g appear in the cases D and E, respectively. The suppliersThe cases A through E will occur depending on the performance parameters of the suppliers and the unit energy prices. The conditions of each case can be obtained from the graphical analysis. For example, the case A occurs if λ1 at the intersection of G and B is smaller than that at the intersection of GT and B, and is smaller than that at the intersection of ST and B. In addition, the line B has to be located above the line AC so that the feasible solution region exists. Then, the following conditions can be derived.(19)(20)(21)Equation (19) means that the gas cost to produce a certain quantity of electricity and steam with the gas turbine is higher than the total of the electricity and oil costs to purchase the same quantity of electricity from the grid and to produce the same quantity of steam with the boiler.Equation (20) means that the electricity cost to purchase a certain quantity of electricity is cheaper than the oil cost to produce the same quantity of electricity using the boiler and the steam turbine. Equation (21) indicates that the reduction of the gas cost by a certain quantity of the inlet air cooling should be smaller than the oil cost to provide the same quantity of cooling using the boiler and the absorption chiller. Otherwise, the optimal solution does not exist because the reduction of the gas cost is unlimited by the inlet air cooling using the absorption chiller driven by the boiler.Figure 2. The possible cases of the optimal solution on the operational condition ISimilar ly, the following conditions can be derived for the other cases. The condition given as Eq. (21) has to be applied to all the cases below.Case B:(22)(23)Equation (22) compares the production cost of the electricity and the steam between the gas and the oil. The gas cost to produce a certain quantity of electricity and steam by the gas turbine is higher than the oil cost to produce the same quantity of electricity and steam by thecombination of the boiler and the steam turbine. Equation (23) is the opposite of Eq. (20), which means that the oil cost to produce a certain quantity of electricity by the boiler and the steam turbine is cheaper than the purchase price of electricity.Case C:(24)(25)(26)(27)Equation (24) is the opposite case of Eq. (19). Equation (25) compares the boiler and the gas turbine regarding the steam production, which is related to the mode d. In the case C, the oil cos t for the boiler is cheaper than the gas cost for the gas turbine to produce a certain quantity of steam. If the gas cost is cheaper, mode d is not a candidate for the optimal sol ution, as illustrated in the case C’. Equations (26) and (27) evaluate the effectiveness of the steam turbine and the inlet air cooling by the absorption chiller,resp ectively. The grid electricity is superior to the steam turbine and to the inlet air cooling in this case.Case D:In addition to Eq. (25),(28)(29)(30)Similarly to the case C’, the case D’ occurs if the inequality sign of Eq. (25) is reversed. Equation (28) is the opposite case of Eq. (22), which is the comparison of the electricity production between gas and oil. Equation (29) is the opposite case of Eq. (26), which is the comparison of the steam turbine and grid electricity. The gas cost to produce a certain quantity of electricity by the combination of the gas turbine and the steam turbine is cheaper than the purchase cost of the same quantity of electricity from the grid. Equation (30) gives the condition where the steam turbine is more advantageous than the inlet air cooling by the absorption chiller. The left hand side of Eq. (30) represents an additional steam required for a certain quantity of electricity production by the inlet air cooling. Therefore, Eq. (30) insists that the steam required for a certain quantity of electricity production by the steam turbine is smaller than that requiredfor the same quantity of electricity production by the inlet air cooling in this case, and it is independent of energy prices.Case E:In addition to Eq.(25),(31)(32)The case E’ occurs if Eq. (25) is reversed. Equations (31) and (32) are the opposite cases of Eqs. (27)and (30), which give the conditions where the inlet air cooling is more advantageous compared with the alternative technologies. In this case, Eq. (28) is always satisfied because of Eqs. (21) and (32).The conditions discussed above can be arranged using the relative electricity price, Pe/Pg and the relative oil price, Po/Pg. The optimal cases to be chosen are graphically shown in Figure 3 on the Po/Pg-Pe/Pg plane. When Eq. (30) is valid, Figure 3 (a) should be applied. The inlet air cooling is not an optimal option in any case. When Eq. (32) is valid, the cases E and E’ appear on the plane and the steam turbine is never chosen, as depicted in Figure 3 (b). It is noteworthy that if the inlet air cooling cannot improve the gas turbine efficiency, i.e. βGT = 0, the inlet air cooling is never the optimal solution.As the cases C, D and E include three operation modes, another criterion for the selection of the optimal operation mode is necessary in those cases. The additional criterion is related with the steam to electricity ratio, and can be derived from the consideration below.In the c ases C, D and E, λ1 and λ2 have positive values. Therefore, two of the constraints given as Eqs. (6) and (7) take the equality conditions due to the Kuhn-Tucker condition Eq. (12). Then, the two equations can be solved simultaneously for two variables which have positive values at each mode.For the mode d, the simultaneous equations can be solved under xGT, xB > 0 and xG, xST, xAC = 0.Then, one can obtain xGT = xe and xB = xs ¡ ρGTxe. Because xB has a positive value, the following condition has to be satisfied for the mode d to be selected.(33)At the mode e, one can obtain xG = xe ¡ xs/ρGT and xGT = xs/ρGT, and the following condition can be drawn out of the former expression because xG is greater than zero at this mode.(34)Similar considerations can be applied to the cases D and E. Consequently, Eq. (33) is the condition for the mode d to be selected, while Eq. (34) is the condition for the modes e, f or g to be selected. Furthermore, it is obvious that the mode c has to be chosen if the steam to electricity ratio of the gas turbine is equal to the ratio of the heat flow rate of the steam demand to the electric power demand, i.e. ρGT = xs/xe.Equations (33) and (34) mean that when the steam to electricity ratio of the gas turbine is smaller than the ratio of the heat flow rate of the steam demand to the electric power demand, the gas turbine should be operated to meet the electric power demand. Then, the boiler should balance the heat flow rate of the steam supply with the demand. On the other hand, if the steam to electricity ratio of the gas turbine is larger than the ratio of the heat flow rate of the steam demand to the electric power demand,the gas turbine has to be operated to meet the heat flow rate of the steam demand. Then, the insufficient electric power supply from the gas turbine has to be compensated by either the grid (mode e), the steam turbine (mode f), or the inlet air cooling (mode g). There is no need of any auxiliary equipment to supply additional electric power or steam if the steam to electricity ratio of the gas turbine matches the demands.Figure 3. The optimal operation cases expressed on the relative oil price-relative electricity price plane (the operational condition I).2.4. The Optimal Solution where the Electric Power from the Gas Turbine is at the MaximumIn the operational condition II, the third constraint, Eq. (8), takes the equality condition and λ3 would have a positive value. Then, Eqs. (11) and (18) yields:(35)It is reasonable to assume that ρGT ¡ !AC ®GT > 0 and ωGT ¡ ¯GT ®GT > 0 in the case ofgas turbine cogeneration systems because of relatively low electric efficiency (¼ 25 %) and a high heat to electricity ratio (ρGT > 1.4). Then, the optimal solution cases c an be defined by a similar consideration to the operational condition I, and the newly appeared cases are illustrated in Figure 4. The cases F and G can occur in the operational condition II in addition to the cases A and B of the operational condition I. Similarly to the cases C’ and D’ of the operational condition I, the cases F’ and G’ can be defined where the mode h is excluded from the cases F and G, respectively.Figure 4. The optimal solution cases on the operational condition II.In the operational condition II, the conditions of the cases A and B are slightly different from those in the operational condition I, as given below.Case A:(36)(37)Case B:(38)(39)The conditions for the cases F and G are obtained as follows.Case F:(40)(41)(42)Case G:In addition to Eq. (41),(43)(44)The case s F’ and G’ occur whenthe inequality sign of Eq. (41) is reversed. Equations (36), (38),(40), (41), (42), (43) and (44) correspond to Eqs. (19), (22), (24), (25), (26), (28) and (29), respectively.In these equations, ωGT ¡ ¯GT®GTis substituted for ωGT, an d ρGT ¡ !AC®GTis substituted for ρGT.The optimal cases of the operational condition II are illustrated on the Po/Pg-Pe/Pg plane as shown in Figure 5. Unlike the operational condition I, there is no lower limit of the relative oil price for the optimal solution to exist. The line separating the cases F and G is determined by the multiple parameters.Basically, a larger ρGT or a smaller ωST lowers the line, which causes a higher possibility for the case G to be selected.Figure 5. The optimal operation cases expressed on the relative oil price-relative electricity price plane (the operational condition II).To find the optimal mode out of three operation modes included in the cases F or G, another strategy is necessary. The additional conditions can be found by a similar examination on the variables to that done for the cases C, D and E. In the operational condition II, three variables can be analytically solved by the constraints given as Eqs. (6), (7) and (8) taking equality conditions.In the mode g, only two variables, ωGT andωAC are positive and the other variables are equal to zero.Therefore, the analytical solutions of those in the operational condition II can be obtained from equations derived from Eqs. (6) and (7) as xGT = xe and xAC = (ρGTxe ¡xs)/ωA C. Then the third constraint gives the equality condition concerning xs/xe and XGT/xe as follows:(45)where, XGT/xe represents the ratio of the gas turbine capacity to the electricity demand, and XGT/xe ·1.For mode h, the condition where this mode should be selected is derived from the analytical solution of xB with xB > 0 as follows:(46)For the mode i, xG > 0 and xAC > 0 give the following two conditions.(47)(48)For the mode j, xST > 0 and xAC > 0 give the following conditions.(49)(50)The conditions given as Eqs. (45–50) are graphically shown in Figure 6. In the cases F and G,the operational condition II cannot be applied to the region of xsxe< ρGTXGT xeand xsxe<(ωST+ρGT)XGTxe¡ωST,respectively, because xAC becomes negative in this region. The optimal operation should be found under the operational condition I in this region.3. Comparison of the Optimal Operation Criteria with a Detailed Optimization ResultTo examine the applicability of the method explained in the previous section to a practical cogeneration system, the combination of the suppliers selected by the optimal operation criteria was compared with the results of a detailed optimization of an existing plant.3.1. An Example of an Existing Energy Center of a FactoryAn energy center of an existing factory is depicted in Figure 7. The factory is located in Aichi Prefecture, Japan, and produces car-related parts. The energy center produces electricity by a combined cycle of a gas turbine and a steam turbine. The gas turbine can be fueled with either gas or kerosene, and it is equipped with an inlet air cooler. The electric power distribution system of the factory is also linked to the electricity grid so that the electricity can be purchased in case the electric power supply from the energy center is insufficient.The steam is produced from the gas turbine and boilers. The high, medium or low pressure steam is consumed in the manufacturing process as well as for the driving force of the steam turbine and absorption chillers. The absorption chillers supply chilled water for the process, air conditioning and the inlet air cooling. One of the absorption chiller can utilize hot water recovered from the low temperature waste gas of the gas turbine to enhance the heat recovery efficiency of the system.Figure 6. The selection of the optimal operation mode in the cases of F and G.3.2. The Performance Characteristics of the EquipmentThe part load characteristics of the equipment were linearly approximated so that the system could be modeled by the linear programming. The approximation lines were derived from the characteristics of the existing machines used in the energy center.The electricity and the steam generation characteristics of the gas turbine and the HRSG are shown in Figure 8, for example. The electric capacity of the gas turbine increases with lower inlet air temperatures. The quantity of generated steam is also augmented with lower inlet air temperatures.In practice, it is known that the inlet air cooling is beneficial when the purchase of the grid electricity will exceed the power contract without the augmentation of the gas turbine capacity. Furthermore, the inlet air cooling is effective when the outdoor air temperature is higher than 11 ◦C. A part of the operation of the actual gas turbine system is based on the above judgement of the operator, which is also included in the detailed optimization model.3.3. The Detailed Optimization of the Energy CenterThe optimization of the system shown in Figure 7 was performed by a software tool developed for this system. The optimization method used in the tool is the linear programming method combined with the listed start-stop patterns of equipment and with the judgement whether the inlet air cooling is on oroff. The methodology used in the tool is fully described in the reference [11].Figure 7. An energy center of a factory.Figure 8. The performance characteristics of the gas turbine and the HRSG.The Detailed Optimization MethodThe energy flow in the energy center was modeled by the linear programming. The outputs of equipment were the variables to be optimized, whose values could be varied within the lower and upper limits. To make the optimization model realistic, it is necessary to take the start-stop patterns of the equipment into account. The start-stop patterns were generated according to thepossible operation conditions of the actual energy center, and 20 patterns were chosen for the enumeration. The optimal solution was searched by the combination of the enumeration of the start-stop patterns and the linear programming method. The list of the start-stop patterns of the gas turbine and the steam turbine is given in Figure 9.The demands given in the detailed optimization are shown in Figure 10 as the ratios of the heat flow rate of the steam demand to the electric power demand on a summer day with a large electric power demand and on a winter day with a small steam demand. On the summer day, the ratio of the heat flow rate of the steam demand to the electric power demand is at a low level throughout a day. While, it is high on the winter day, and during the hours 2 to 6, the ratio exceeds 1.4 that is the steam to electricity ratio of the gas turbine.Figure 9. The start-stop patterns of the gas turbine and the steam turbine.The Plant Operation Obtained by the Detailed OptimizationThe accumulated graphs shown in Figures 11 through 14 illustrate the electric power supply and the heat flow rate of the steam supply from equipment on the summer and winter days. On the summer day, the gas turbine and the steam turbine worked at the maximum load and the electric power demand was met by the purchase from the grid for most of the day except the hours 2 to 6, at which the electric power demand was small. The inlet air cooling of the gas turbine was used only at the hours 10 and 14, at which the peak of the electric power demand existed. The steam was mainly supplied by the gas turbine, and the boiler was used only if the total heat flow rate of the steam demands by the process, the steam turbine, and the absorption。
控制系统介绍外文文献翻译、中英文翻译、外文翻译
Introductions to Control SystemsAutomatic control has played a vital role in the advancement of engineering and science. In addition to its extreme importance in space-vehicle, missile-guidance, and aircraft-piloting systems, etc, automatic control has become an important and integral part of modern manufacturing and industrial processes. For example, automatic control is essential in such industrial operations as controlling pressure, temperature, humidity, viscosity, and flow in the process industries; tooling, handling, and assembling mechanical parts in the manufacturing industries, among many others.Since advances in the theory and practice of automatic control provide means for attaining optimal performance of dynamic systems, improve the quality and lower the cost of production, expand the production rate, relieve the drudgery of many routine, repetitive manual operations etc, most engineers and scientists must now have a good understanding of this field.The first significant work in automatic control was James Watt’s centrifugal governor for the speed control of a steam engine in the eighteenth century. Other significant works in the early stages of development of control theory were due to Minorsky, Hazen, and Nyquist, among many others. In 1922 Minorsky worked on automatic controllers for steering ships and showed how stability could be determined by the differential equations describing the system. In 1934 Hazen, who introduced the term “ervomechanisms”for position control systems, discussed design of relay servomechanisms capable of closely following a changing input.During the decade of the 1940’s, frequency-response methods made it possible for engineers to design linear feedback control systems that satisfied performance requirements. From the end of the 1940’s to early 1950’s, the root-locus method in control system design was fully developed.The frequency-response and the root-locus methods, which are the core of classical theory, lead to systems that are stable and satisfy a set of more or less arbitrary performance requirements. Such systems are, ingeneral, not optimal in any meaningful sense. Since the late 1950’s, the emphasis on control design problems has been shifted from the design of one of many systems that can work to the design of one optimal system in some meaningful sense.As modern plants with many inputs and outputs become more and more complex, the description of a modern control system requires a large number of equations. Classical control theory, which deals only with single-input-single-output systems, becomes entirely powerless for multiple-input-multiple-output systems. Since about 1960, modern control theory has been developed to cope with the increased complexity of modern plants and the stringent requirements on accuracy, weight, and industrial applications.Because of the readily available electronic analog, digital, and hybrid computers for use in complex computations, the use of computers in the design of control systems and the use of on-line computers in the operation of control systems are now becoming common practice.The most recent developments in modern control theory may be said to be in the direction of the optimal control of both deterministic and stochastic systems as well as the adaptive and learning control of complex systems. Applications of modern control theory to such nonengineering fields as biology, economics, medicine, and sociology are now under way, and interesting and significant results can be expected in the near future.Next we shall introduce the terminology necessary to describe control systems.Plants. A plant is a piece of equipment, perhaps just a set of machine parts functioning together, the purpose of which is to perform a particular operation. Here we shall call any physical object to be controlled (such as a heating furnace, a chemical reactor, or a spacecraft) a plant.Processes. The Merriam-Webster Dictionary defines a process to be a natural, progressively continuing operation or development marked by a series of gradual changes that succeed one another in a relatively fixed way and lead toward a particular result or end; or an artificial or voluntary, progressively continuing operation that consists of a series of controlledactions or movements systematically directed toward a particular result or end.Here we shall call any operation to be controlled a process. Examples are chemical, economic, and biological process.Systems. A system is a combination of components that act together and perform a certain objective. A system is not limited to abstract, dynamic phenomena such as those encountered in economics. The word “system” should, therefore, be interpreted to imply physical, biological, economic, etc., system.Disturbances. A disturbance is a signal which tends to adversely affect the value of the output of a system. If a disturbance is generated within the system, it is called internal, while an external disturbance is generated outside the system and is an input.Feedback control.Feedback control is an operation which, in the presence of disturbances, tends to reduce the difference between the output of a system and the reference input (or an arbitrarily varied, desired state) and which does so on the basis of this difference. Here, only unpredictable disturbance (i.e., those unknown beforehand) are designated for as such, since with predictable or known disturbances, it is always possible to include compensation with the system so that measurements are unnecessary.Feedback control systems. A feedback control system is one which tends to maintain a prescribed relationship between the output and the reference input by comparing these and using the difference as a means of control.Note that feedback control systems are not limited to the field of engineering but can be found in various nonengineering fields such as economics and biology. For example, the human organism, in one aspect, is analogous to an intricate chemical plant with an enormous variety of unit operations.The process control of this transport and chemical-reaction network involves a variety of control loops. In fact, human organism is an extremely complex feedback control system.Servomechanisms. A servomechanism is a feedback control system in which the output is some mechanical position, velocity, or acceleration. Therefore, the terms servomechanism and position- (or velocity- oracceleration-) control system are synonymous. Servomechanisms are extensively used in modern industry. For example, the completely automatic operation of machine tools, together with programmed instruction, may be accomplished by use of servomechanisms.Automatic regulating systems. An automatic regulating system is a feedback control system in which the reference input or the desired output is either constant or slowly varying with time and in which the primary task is to maintain the actual output at the desired value in the presence of disturbances.A home heating system in which a thermostat is the controller is an example of an automatic regulating system. In this system, the thermostat setting (the desired temperature) is compared with the actual room temperature. A change in the desired room temperature is a disturbance in this system. The objective is to maintain the desired room temperature despite changes in outdoor temperature. There are many other examples of automatic regulating systems, some of which are the automatic control of pressure and of electric quantities such as voltage, current and frequency.Process control systems. An automatic regulating system in which the output is a variable such as temperature, pressure, flow, liquid level, or pH is called a process control system.Process control is widely applied in industry. Programmed controls such as the temperature control of heating furnaces in which the furnace temperature is controlled according to a preset program are often used in such systems. For example, a preset program may be such that the furnace temperature is raised to a given temperature in a given time interval and then lowered to another given temperature in some other given time interval. In such program control the set point is varied according to the preset time schedule. The controller then functions to maintain the furnace temperature close to the varying set point. It should be noted that most process control systems include servomechanisms as an integral part.控制系统介绍自动控制在工程学和科学的推进扮演一个重要角色。
通风中英文对照
采暖通风与空气调节术语标准中英文对照2009-11-29 11:37AA-weighted sound pressure level A声级absolute humidity绝对湿度absolute roughness绝对粗糙度absorbate 吸收质absorbent 吸收剂absorbent吸声材料absorber吸收器absorptance for solar radiation太阳辐射热吸收系数absorption equipment吸收装置absorption of gas and vapor气体吸收absorptiong refrige rationg cycle吸收式制冷循环absorption-type refrigerating machine吸收式制冷机access door检查门acoustic absorptivity吸声系数actual density真密度actuating element执行机构actuator执行机构adaptive control system自适应控制系统additional factor for exterior door外门附加率additional factor for intermittent heating间歇附加率additional factor for wind force高度附加率additional heat loss风力附加率adiabatic humidification附加耗热量adiabatic humidiflcation绝热加湿adsorbate吸附质adsorbent吸附剂adsorber吸附装置adsorption equipment吸附装置adsorption of gas and vapor气体吸附aerodynamic noise空气动力噪声aerosol气溶胶air balance风量平衡air changes换气次数air channel风道air cleanliness空气洁净度air collector集气罐air conditioning空气调节air conditioning condition空调工况air conditioning equipment空气调节设备air conditioning machine room空气调节机房air conditioning system空气调节系统air conditioning system cooling load空气调节系统冷负荷air contaminant空气污染物air-cooled condenser风冷式冷凝器air cooler空气冷却器air curtain空气幕air cushion shock absorber空气弹簧隔振器air distribution气流组织air distributor空气分布器air-douche unit with water atomization喷雾风扇air duct风管、风道air filter空气过滤器air handling equipment空气调节设备air handling unit room空气调节机房air header集合管air humidity空气湿度air inlet风口air intake进风口air manifold集合管air opening风口air pollutant空气污染物air pollution大气污染air preheater空气预热器air return method回风方式air return mode回风方式air return through corridor走廊回风air space空气间层air supply method送风方式air supply mode送风方式air supply (suction) opening with slide plate插板式送（吸）风口air supply volume per unit area单位面积送风量air temperature空气温度air through tunnel地道风air-to-air total heat exchanger全热换热器air-to-cloth ratio气布比air velocity at work area作业地带空气流速air velocity at work place工作地点空气流速air vent放气阀air-water systen空气—水系统airborne particles大气尘air hater空气加热器airspace空气间层alarm signal报警信号ail-air system全空气系统all-water system全水系统allowed indoor fluctuation of temperature and relative humidity室内温湿度允许波动范围ambient noise环境噪声ammonia氨amplification factor of centrolled plant调节对象放大系数amplitude振幅anergy@angle of repose安息角ange of slide滑动角angle scale热湿比angle valve角阀annual [value]历年值annual coldest month历年最冷月annual hottest month历年最热月anticorrosive缓蚀剂antifreeze agent防冻剂antifreeze agent防冻剂apparatus dew point机器露点apparent density堆积密度aqua-ammonia absorptiontype-refrigerating machine氨—水吸收式制冷机aspiation psychrometer通风温湿度计Assmann aspiration psychrometer通风温湿度计atmospheric condenser淋激式冷凝器atmospheric diffusion大气扩散atmospheric dust大气尘atmospheric pollution大气污染atmospheric pressure大气压力（atmospheric stability大气稳定度atmospheric transparency大气透明度atmospheric turblence大气湍流automatic control自动控制automatic roll filter自动卷绕式过滤器automatic vent自动放气阀available pressure资用压力average daily sol-air temperature日平均综合温度axial fan轴流式通风机azeotropic mixture refrigerant共沸溶液制冷剂Bback-flow preventer防回流装置back pressure of steam trap凝结水背压力back pressure return余压回水background noise背景噪声back plate挡风板bag filler袋式除尘器baghouse袋式除尘器barometric pressure大气压力basic heat loss基本耗热量hend muffler消声弯头bimetallic thermometer双金属温度计black globe temperature黑球温度blow off pipe排污管blowdown排污管boiler锅炉boiller house锅炉房boiler plant锅炉房boiler room锅炉房booster加压泵branch支管branch duct(通风) 支管branch pipe支管building envelope围护结构building flow zones建筑气流区building heating entry热力入口bulk density堆积密度bushing补心butterfly damper蝶阀by-pass damper空气加热器〕旁通阀by-pass pipe旁通管Ccanopy hood 伞形罩capillary tube毛细管capture velocity控制风速capture velocity外部吸气罩capturing hood 卡诺循环Carnot cycle串级调节系统cascade control system铸铁散热器cast iron radiator催化燃烧catalytic oxidation 催化燃烧ceilling fan吊扇ceiling panelheating顶棚辐射采暖center frequency中心频率central air conditionint system 集中式空气调节系统central heating集中采暖central ventilation system新风系统centralized control集中控制centrifugal compressor离心式压缩机entrifugal fan离心式通风机check damper(通风〕止回阀check valve止回阀chilled water冷水chilled water system with primary-secondary pumps一、二次泵冷水系统chimney(排气〕烟囱circuit环路circulating fan风扇circulating pipe循环管circulating pump循环泵clean room洁净室cleaning hole清扫孔cleaning vacuum plant真空吸尘装置cleanout opening清扫孔clogging capacity容尘量close nipple长丝closed booth大容积密闭罩closed full flow return闭式满管回水closed loop control闭环控制closed return闭式回水closed shell and tube condenser卧式壳管式冷凝器closed shell and tube evaporator卧式壳管式蒸发器closed tank闭式水箱coefficient of accumulation of heat蓄热系数coefficient of atmospheric transpareney大气透明度coefficient of effective heat emission散热量有效系数coficient of effective heat emission传热系数coefficient of locall resistance局部阻力系数coefficient of thermal storage蓄热系数coefficient of vapor蒸汽渗透系数coefficient of vapor蒸汽渗透系数coil盘管collection efficiency除尘效率combustion of gas and vapor气体燃烧comfort air conditioning舒适性空气调节common section共同段compensator补偿器components(通风〕部件compression压缩compression-type refrigerating machine压缩式制冷机compression-type refrigerating system压缩式制冷系统compression-type refrigeration压缩式制冷compression-type refrigeration cycle压缩式制冷循环compression-type water chiller压缩式冷水机组concentratcd heating集中采暖concentration of narmful substance有害物质浓度condensate drain pan凝结水盘condensate pipe凝结水管condensate pump凝缩水泵condensate tank凝结水箱condensation冷凝condensation of vapor气体冷凝condenser冷凝器condensing pressure冷凝压力condensing temperature冷凝温度condensing unit压缩冷凝机组conditioned space空气调节房间conditioned zone空气调节区conical cowl锥形风帽constant humidity system恒湿系统constant temperature and humidity system恒温恒湿系统constant temperature system 恒温系统constant value control 定值调节constant volume air conditioning system定风量空气调节系统continuous dust dislodging连续除灰continuous dust dislodging连续除灰continuous heating连续采暖contour zone稳定气流区control device控制装置control panel控制屏control valve调节阀control velocity控制风速controlled natural ventilation有组织自然通风controlled plant调节对象controlled variable被控参数controller调节器convection heating对流采暖convector对流散热器cooling降温、冷却（、）cooling air curtain冷风幕cooling coil冷盘管cooling coil section冷却段cooling load from heat传热冷负荷cooling load from outdoor air新风冷负荷cooling load from ventilation新风冷负荷cooling load temperature冷负荷温度cooling system降温系统cooling tower冷却塔cooling unit冷风机组cooling water冷却水correcting element调节机构correcting unit执行器correction factor for orientaion朝向修正率corrosion inhibitor缓蚀剂coupling管接头cowl伞形风帽criteria for noise control cross噪声控频标准cross fan四通crross-flow fan贯流式通风机cross-ventilation穿堂风cut diameter分割粒径cyclone旋风除尘器cyclone dust separator旋风除尘器cylindrical ventilator筒形风帽Ddaily range日较差damping factot衰减倍数data scaning巡回检测days of heating period采暖期天数deafener消声器decibel(dB)分贝degree-days of heating period采暖期度日数degree of subcooling过冷度degree of superheat过热度dehumidification减湿dehumidifying cooling减湿冷却density of dust particle真密度derivative time微分时间design conditions计算参数desorption解吸detecting element检测元件detention period延迟时间deviation偏差dew-point temperature露点温度dimond-shaped damper菱形叶片调节阀differential pressure type flowmeter差压流量计diffuser air supply散流器diffuser air supply散流器送风direct air conditioning system 直流式空气调节系统direct combustion 直接燃烧direct-contact heat exchanger 汽水混合式换热器direct digital control (DDC) system 直接数字控制系统direct evaporator 直接式蒸发器direct-fired lithiumbromide absorption-type refrigerating machine 直燃式溴化锂吸收式制冷机direct refrigerating system 直接制冷系统direct return system 异程式系统direct solar radiation 太阳直接辐射discharge pressure 排气压力discharge temperature 排气温度dispersion 大气扩散district heat supply 区域供热district heating 区域供热disturbance frequency 扰动频率dominant wind direction 最多风向double-effect lithium-bromide absorption-type refigerating machine 双效溴化锂吸收式制冷机double pipe condenser 套管式冷凝器down draft 倒灌downfeed system 上分式系统downstream spray pattern 顺喷drain pipe 泄水管drain pipe 排污管droplet 液滴drv air 干空气dry-and-wet-bulb thermometer 干湿球温度表dry-bulb temperature 干球温度dry cooling condition 干工况dry dust separator 干式除尘器dry expansion evaporator 干式蒸发器dry return pipe 干式凝结水管dry steam humidifler 干蒸汽加湿器dualductairconing ition 双风管空气调节系统dual duct system 双风管空气调节系统duct 风管、风道dust 粉尘dust capacity 容尘量dust collector 除尘器dust concentration 含尘浓度dust control 除尘dust-holding capacity 容尘量dust removal 除尘dust removing system 除尘系统dust sampler 粉尘采样仪dust sampling meter 粉尘采样仪dust separation 除尘dust separator 除尘器dust source 尘源dynamic deviation动态偏差Eeconomic resistance of heat transfer经济传热阻economic velocity经济流速efective coefficient of local resistance折算局部阻力系数effective legth折算长度effective stack height烟囱有效高度effective temperature difference送风温差ejector喷射器ejetor弯头elbow电加热器electric heater电加热段electric panel heating电热辐射采暖electric precipitator电除尘器electricradian theating 电热辐射采暖electricresistance hu-midkfier电阻式加湿器electro-pneumatic convertor电—气转换器electrode humidifler电极式加湿器electrostatic precipi-tator电除尘器eliminator挡水板emergency ventilation事故通风emergency ventilation system事故通风系统emission concentration排放浓度enclosed hood密闭罩enthalpy焓enthalpy control system新风〕焓值控制系统enthalpy entropy chart焓熵图entirely ventilation全面通风entropy熵environmental noise环境噪声equal percentage flow characteristic等百分比流量特性equivalent coefficient of local resistance当量局部阻力系数equivalent length当量长度equivalent[continuous A] sound level等效〔连续A〕声级evaporating pressure蒸发压力evaporating temperature蒸发温度evaporative condenser蒸发式冷凝器evaporator蒸发器excess heat余热excess pressure余压excessive heat 余热cxergy@exhaust air rate排风量exhaust fan排风机exhaust fan room排风机室exhaust hood局部排风罩exhaust inlet吸风口exhaust opening吸风口exhaust opening orinlet风口exhaust outlet排风口exaust vertical pipe排气〕烟囱exhausted enclosure密闭罩exit排风口expansion膨胀expansion pipe膨胀管explosion proofing防爆expansion steam trap恒温式疏水器expansion tank膨胀水箱extreme maximum temperature极端最高温度extreme minimum temperature极端最低温度Ffabric collector袋式除尘器face tube皮托管face velocity罩口风速fan通风机fan-coil air-conditioning system风机盘管空气调节系统fan-coil system风机盘管空气调节系统fan-coil unit风机盘管机组fan house通风机室fan room通风机室fan section风机段feed-forward control前馈控制feedback反馈feeding branch tlo radiator散热器供热支管fibrous dust纤维性粉尘fillter cylinder for sampling滤筒采样管fillter efficiency过滤效率fillter section过滤段filltration velocity过滤速度final resistance of filter过滤器终阻力fire damper防火阀fire prevention防火fire protection防火fire-resisting damper防火阀fittings(通风〕配件fixed set-point control定值调节fixed support固定支架fixed time temperature (humidity)定时温（湿）度flame combustion热力燃烧flash gas闪发气体flash steam二次蒸汽flexible duct软管flexible joint柔性接头float type steam trap浮球式疏水器float valve浮球阀floating control无定位调节flooded evaporator满液式蒸发器floor panel heating地板辐射采暖flow capacity of control valve调节阀流通能力flow characteristic of control valve调节阀流量特性foam dust separator泡沫除尘器follow-up control system随动系统forced ventilation机械通风forward flow zone射流区foul gas不凝性气体four-pipe water system四管制水系统fractional separation efficiency分级除尘效率free jet自由射流free sillica游离二氧化硅free silicon dioxide游离二氧化硅freon氟利昂frequency interval频程frequency of wind direction风向频率fresh air handling unit新风机组resh air requirement新风量friction factor摩擦系数friction loss摩擦阻力frictional resistance摩擦阻力fume烟〔雾〕fumehood排风柜fumes烟气Ggas-fired infrared heating 煤气红外线辐射采暖gas-fired unit heater 燃气热风器gas purger 不凝性气体分离器gate valve 闸阀general air change 全面通风general exhaust ventilation (GEV) 全面排风general ventilation 全面通风generator 发生器global radiation总辐射grade efficiency分级除尘效率granular bed filter颗粒层除尘器granulometric distribution粒径分布gravel bed filter颗粒层除尘器gravity separator沉降室ground-level concentration落地浓度guide vane导流板Hhair hygrometor毛发湿度计hand pump手摇泵harmful gas andvapo有害气体harmful substance有害物质header分水器、集水器（、）heat and moisture热湿交换transfer热平衡heat conduction coefficient导热系数heat conductivity导热系数heat distributing network热网heat emitter散热器heat endurance热稳定性heat exchanger换热器heat flowmeter热流计heat flow rate热流量heat gain from lighting设备散热量heat gain from lighting照明散热量heat gain from occupant人体散热量heat insulating window保温窗heat(thermal)insuation隔热heat(thermal)lag延迟时间heat loss耗热量heat loss by infiltration冷风渗透耗热量heat-operated refrigerating system热力制冷系统heat-operated refrigetation热力制冷heat pipe热管heat pump热泵heat pump air conditioner热泵式空气调节器heat release散热量heat resistance热阻heat screen隔热屏heat shield隔热屏heat source热源heat storage蓄热heat storage capacity蓄热特性heat supply供热heat supply network热网heat transfer传热heat transmission传热heat wheel转轮式换热器heated thermometer anemometer热风速仪heating采暖、供热、加热（、、）heating appliance采暖设备heating coil热盘管heating coil section加热段heating equipment采暖设备heating load热负荷heating medium热媒heating medium parameter热媒参数heating pipeline采暖管道heating system采暖系统heavy work重作业high-frequency noise高频噪声high-pressure ho twater heating高温热水采暖high-pressure steam heating高压蒸汽采暖high temperature water heating高温热水采暖hood局部排风罩horizontal water-film syclonet卧式旋风水膜除尘器hot air heating热风采暖hot air heating system热风采暖系统hot shop热车间hot water boiler热水锅炉hot water heating热水采暖hot water system热水采暖系统hot water pipe热水管hot workshop热车间hourly cooling load逐时冷负荷hourly sol-air temperature逐时综合温度humidification加湿humidifier加湿器humididier section加湿段humidistat恒湿器humidity ratio含湿量hydraulic calculation水力计算hydraulic disordeer水力失调hydraulic dust removal水力除尘hydraulic resistance balance阻力平衡hydraulicity水硬性hydrophilic dust亲水性粉尘hydrophobic dust疏水性粉尘Iimpact dust collector冲激式除尘器impact tube皮托管impedance muffler阻抗复合消声器inclined damper斜插板阀index circuit最不利环路indec of thermal inertia (valueD)热惰性指标（D值）indirect heat exchanger表面式换热器indirect refrigerating sys间接制冷系统indoor air design conditions室内在气计算参数indoor air velocity室内空气流速indoor and outdoor design conditions室内外计算参数indoor reference for air temperature and relative humidity室内温湿度基数indoor temperature (humidity)室内温（湿）度induction air-conditioning system诱导式空气调节系统induction unit诱导器inductive ventilation诱导通风industral air conditioning工艺性空气调节industrial ventilation工业通风inertial dust separator惯性除尘器infiltration heat loss冷风渗透耗热量infrared humidifier红外线加湿器infrared radiant heater红外线辐射器inherent regulation of controlled plant调节对象自平衡initial concentration of dust初始浓度initial resistance of filter过滤器初阻力imput variable输入量insulating layer保温层integral enclosure整体密闭罩integral time积分时间interlock protection联锁保护intermittent dust removal定期除灰intermittent heating间歇采暖inversion layer逆温层inverted bucket type steam trap倒吊桶式疏水器irradiance辐射照度isoenthalpy等焓线isobume等湿线isolator隔振器isotherm等温线isothermal humidification等温加湿isothermal jet等温射流Jjet射流jet axial velocity射流轴心速度jet divergence angle射流扩散角jet in a confined space受限射流katathermometer卡他温度计Llaboratory hood排风柜lag of controlled plant调节对象滞后large space enclosure大容积密闭罩latent heat潜热lateral exhaust at the edge of a bath槽边排风罩lateral hoodlength of pipe section侧吸罩length of pipe section管段长度light work轻作业limit deflection极限压缩量limit switch限位开关limiting velocity极限流速linear flow characteristic线性流量特性liquid-level gage液位计liquid receiver贮液器lithium bromide溴化锂lithium-bromide absorption-type refrigerating machine溴化锂吸收式制冷机lithium chloride resistance hygrometer氯化锂电阻湿度计load pattern负荷特性local air conditioning局部区域空气调节local air suppiy system局部送风系统local exhaustventilation (LEV)局部排风local exhaust system局部排风系统local heating局部采暖local relief局部送风local relief system局部送风系统local resistance局部。
- 1、下载文档前请自行甄别文档内容的完整性，平台不提供额外的编辑、内容补充、找答案等附加服务。
- 2、"仅部分预览"的文档,不可在线预览部分如存在完整性等问题,可反馈申请退款(可完整预览的文档不适用该条件!)。
- 3、如文档侵犯您的权益，请联系客服反馈,我们会尽快为您处理(人工客服工作时间：9:00-18:30)。
热风炉控制系统中英文对照外文翻译文献(文档含英文原文和中文翻译)译文:基于西门子PCS7的热风炉控制系统的设计本文介绍的方法利用西门子过程控制系统PCS7 V6.0控制加热炉。
描述了两者的配置控制系统软件和硬件，功能通过该系统，随着困难解决方案。
加热炉控制系统的配置双CPU冗余。
采用工业以太网，欧洲流行的PROFIBUS DP现场总线和分布式I / O减反射膜结构。
它采用ET200M I/O站的冗余。
带PROFIBUS-DP通信接口和节点具有双控制器的通信协议（CPU）。
一、介绍在生产过程中的热轧带钢，要求对来料板坯温度比较高；一般来说，应当是1 350℃左右。
的加热炉的加热程序的设备，如能满足连续可靠的要求生产只有在控制的温度和输出量有很好的协调。
加热炉采用可移动的步进梁移动冷板坯的出口侧的输入时，炉侧；钢板坯是移动的，它将被加热的喷嘴喷射炉气联合焦炭炉。
当板坯入炉炉体的末端，它首先会被加热到850℃左右在预热段，然后约1300℃在加热段；最后将进入热浸泡部分使板坯加热均匀滚动。
上述控制过程通常通过不断的PID （比例，积分和差分）。
S分别对各控制截面的顶部或侧壁分别收集实际温度在每节该炉和再采样值将被发送到PLC（可编程逻辑控制器）实现连续比例，积分和微分（PID控制）通过测量值之间的差异空气和煤气流量设定值；然后开度每段的喷枪将调整控制气体的流量，温度控制，然而，因为它不是关于气体的燃烧清楚，如果这采用的方法是，热利用效率介质的极低、能耗非常大。
在这里，一种改进的双交叉振幅限制全自动燃烧控制进行了介绍和其基本原理是进行控制燃烧的上部和下部各节在正常工作时间；如有必要，温度将上部调整信号可被视为套双交叉限幅控制和在下部前温度检测值可用于炉状态监测。
这一原则主从控制模式可以更好地协调在上燃烧和供热平衡段和下部的燃烧上、下段均匀；同时，它认为天然气的燃烧，起到了很好的作用节能。
在这个项目中，PCS7 V6.0由西门子将用于实现上述控制功能。
二、简要介绍了PCS7系统PCS7过程控制系统是一种先进的定位系列可编程逻辑控制器和TELEPERM通过西门子结合最系列机器人系统先进的计算机软件和硬件技术，采用可更换的操作站，强关系过程控制站与大容量和冗余分布式I/O总线的过程控制系统现场总线技术。
PCS7已被应用在越来越多的行业控制区作为一种面向过程的软件开发平台。
它提出了一种完全集成的自动化解决方案，可以提供所有种类的一个统一的自动化应用技术环境。
以下项目包括它：统一的数据管理，通信，配置和编程软件。
基于环境以上，各种技术可以集成在一个在相同的全球数据库系统整体界面与用户。
工程师或技术人员可以配置和在同一平台上的各种应用程序。
复杂的工程是通过使用一个简单的组态平台。
PCS7使PLC 纳入DCS系统更容易，体现真正的特征的计算机自动控制。
三、简要介绍热风炉控制系统在复杂的工业过程系统，我们总是遇到这样的问题：多个约束条件的多变量系统：强耦合的非线性系统：大；时间延迟；多目标控制；等等。
自定义控件技术无法解决上述问题。
但先进控制技术可以很好的解决上述问题。
怎么用在工业过程中应用先进控制技术产生的实用性是一个迫切需要解决的问题工业自动化研究领域。
根据计算机技术的奔腾，硬件技术，网络技术，先进控制技术的产业化技术是可以实现的。
本文提出了有用的容易实现可靠的控制方式实现步进式加热炉自动控制系统，对的基础上，包括过程控制理论，DCS和PLC技术，通信，现场总线，在步进式加热的特点炉，采用电气、仪表控制设备与技术实用、可靠和指标先进。
我们可以实现仪表控制系统利用DCS和PLC电气控制系统。
控制加热炉系统分为加热炉区PLC控制系统，PLC控制系统和加热辊炉DCS控制系统。
仪表控制器电气连接的操作员站服务器IEEE以太网，采用DCS和PLC技术，网络和现场总线技术相结合的过程控制系统和过程计算机，智能仪器，实现仪器的驱动系统在一个系统的电气控制。
四、热风炉控制系统的组成1.控制系统配置在本文中，基于步进式加热炉控制过程中，控制系统是一个复杂的传热和字符的过程中，有许多特点如干扰，强耦合，大纯滞后等我们讨论的基础上的专用控制装置的设计步进式加热炉在细节包括的特点，相关的软件和硬件信息实现的控制。
PID控制是综合控制规律仪表控制系统，因为它的成熟，熟悉在技术员和操作工，效果好，广泛的应用计算机数据控制设备，特别是复杂的控制系统，实践证明它适应各种工业过程控制。
加热炉的关键设备：装载机机，卸船机，行走系统，系列转换辊，燃烧和跟踪板控制系统。
的蓄热式加热炉的控制系统采用双CPU冗余，冗余环工业以太网，Profibus DP总线和分布式I / O减反射膜结构，显示的详细配置图1。
利用该系统，可以进行传输测量和加权函数，跟踪检测，加载和卸载板，我们可以燃烧和彼此间交换数据来控制过程在所有产品线的轨道板和管理过程。
加热炉的生产工艺如高目标产量，低消耗和污染，自动操作模式的实现。
2.硬件配置如图1所示，在整个DCS控制系统加热炉有两个显著的特点：的第一个是基础自动化级采用冗余环结构，从而提高可靠性和系统的稳定性；第二，信息层采用标准的以太网结构使整个系统的大容量数据通信能力和方便的可扩展性。
针对上述特点以下模式通过硬件的选择：（1）选择过程控制器中cpu414-h由西门子S7-400系列的核心的加热炉控制系统共同构成了冗余系统的控制站与分布I/O ET200M；（2）监控系统采用研华工业控制计算机和菲利普22“纯平彩色显示器工程师站和操作员站。
操作该系统的站在形式的在线工作协调和他们是全透明、全容错，实现彼此的更换。
这种模式使得本系统有利于可靠操作，数据分布合理，操作快捷速度，人机界面友好，使用方便等。
（3）三层网络体系结构的组成标准的以太网（IEEE以太网802。
×），西门子SIMATIC NET工业以太网和现场总线过程现场总线（EN50170）保证了高可靠性，无堵塞和高速度（10M ~ 100米）的数据尤其是在系统，通信，它采用双环容错光纤网络，更有效地保证现场抗干扰能力和的网络的数据传输可靠性高系统。
它采用Windows2000作为微软（英文）操作系统软件和PCS7工具集V6.3由西门子将组态在工程师站作为软件控制计算机和下位监控上位计算机。
此外，它是具有工业以太网s7-redconnect通信软件和冗余系统软件。
操作员站设置上的位置计算机监控软件pcs7wincc，这是通过西门子和微软合作开发。
此外，可以通过共同实现的功能监控软件，pcs7wincc可以加入各种控制和C脚本程序，VB程序实现更复杂的功能。
B.功能的控制系统的实现为了使操作人员掌握操作在计算机控制系统的总体状况时间，准确的控制系统的稳定运行操作方便，本系统建立了系统工艺流程装配图，汽包工艺流程图，加热段和一个过程的流程图热节。
随着工业控制参数的画面，生动地反映该系统的生产过程的状态和提供对检测点的测量值的显示系统。
此外，该系统还建立了环显示图片和集中控制各回路可在环图实现。
单击“详细信息包括设定值，过程值，输出值，自动和手动开关，上下限报警过程变量对PID控制面板。
模拟数量显示值和累积流量的模拟在形式的集中量。
温度计显示系统的主要参数。
解释根据控制系统功能装载自动运行程序流程。
图2。
对加热炉的燃料混合气高炉、焦炉，热值不稳定，在以上的温度控制难度。
在这项目，加热炉的控制方法温度和煤气流量和空气流量级联双交叉限幅方法控制设定值稳定在10℃±。
具体思路如下：以温度该加热炉的主回路，煤气流和空气流作为辅助回路，输出的加热炉的温度控制回路将转化为煤气流的初始设定值空气流量。
在煤气流量的控制将在高和低的选择根据空气流量将受到限幅根据高、低限的煤气流量等确定煤气流回路最终设定值。
的在空气流量控制将受到高和低根据煤气流量的选择，将受到对限幅根据较高和较低的空气流动的限制，确定最终的设定值空气流动回路。
对加热温度的控制原理炉，煤气流量和空气流量串级双交叉限幅图3所示：五、应用中的体会目前现有的高速发展科学和技术，以提高自动化水平和减少劳动工人的强度，应用计算机和过程控制和监测的一些庞大而复杂的过程控制工业系统软件已经发展的一个必然趋势。
在编程的过程中，强PCS7控制流程图的作用（CFC）使程序员可以方便、快速。
唯一的不足是有模块的参数太多的选项，在的情况下，一个恰到好处的PID模块，可以满足需要控制可以开发，规划将更便捷、完善的。
WinCC喇叭进行语音报警功能配置更容易和更快。
这仅仅是必要的记录*。
wav文件的语音报警和连接在喇叭功能的语音报警和报警事件。
在WinCC和Step7股票组合的上位机监控和一些职责收集现场数据合理，发挥各自的不同的设施优势，而应该是计算机的设计特点和前景控制系统。
在系统调试过程和放投入运行，硬件设备的诊断功能PCS7是强大的，他们可以帮助现场调试工程师解决问题快。
控制面板的信息内容全面。
在PID参数的整定过程，可以观察在PV值和OP值和现场操作者改变可以操作的循环相关参数，节省开发人员的时间的量大。
参考文献：1.西门子PCS7用户手册，银，20032.西门子公司配置硬件和通信。
连接PCS7 V6.0手册，20023.jaklic安东。
在铸坯传热模拟运输[J]，应用热工程，2002，4.荷兰足球的发展和计算机在线控制性能在一个三区加热炉[J]，钢铁工程师1982,59（1），44-52.5.弗莱德shenvar内陆。
在步进梁式加热炉监控80热连轧机[J]，钢铁工程师，1987,64（3），23日至24日]6.图瓦E，瓦斯奎斯f.real-time现场总线通信中的应用PROFIBUS网络。
7.B.波特，A.琼斯遗传调谐数字PID控制器。
电子信件，1992，vol.28:843-8448.j.l.tong，j.p鲍勃。
数字PID控制器的设计模型工业电子，控制，仪器仪表和自动化，1992国际会议的程序，1992，第3卷：1157-11629.Y. Huang，s.yasunbu。
一般的PID实用设计方法从传统的PID控制。
第九届IEEE 国际会议上，2000，vol.2:969-97210.保罗哈蒙。
等。
专家系统工具和应用程序，约翰威利和sons.inc，世界图书出版公司，199011.等k J，低t.pid控制器：理论，设计与调整。
纽约：ISA，199512.Mann G K I G，轮毂，高斯林R G.分析直接作用模糊PID控制器结构。
IEEE交易对系统，人，与控制，1999，29b：371-38813.西门子ag.simatic微机用户手册[Z]。
2000。
14.过程控制系统PCS7图书馆siemensag，2003。