锅炉系统毕业论文外文翻译

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锅炉专业词汇英汉对照

A List of Abbreviations and Symbols in English-ChineseA Ash Handling System 除灰系统AH Air Heater 空气预热器AAh Analyzer, Alarm High 分析器，高值报警AIV Air Intake Valve 进气阀ALIGN Alignment 校正ALKF Airlock Feeder 锁气器AP Ash Slurry Pump 灰浆泵ATM Atmosphere 大气AC Air Conditioner 空气调节器AFT Atmosphere Flash Tank 大气扩容器AC Alternating Current 交流电ALM Alarm 报警AMP Ampere 安培AX THR BRG Axis Thrust Bearing 轴向推力，轴承ATMZ Atomizing 雾化AUTO Automation 自动AUX Auxiliary 辅助的BA Bottom Ash 底灰BAH Bottom Ash Hopper 底灰斗BLR Boiler 锅炉BSD Boiler Shut Down 停炉BUSH Bushing 衬套BYPS Bypass 旁路BCP Boiler Circulating Pump 锅炉循环泵BVD Boiler Vents and Drains 锅炉疏水放气BFP Boiler Feed-water Pump 锅炉给水泵BFPTBoiler Feed-water Pump Turbine锅炉给水泵汽机BFW Boiler Feed-water 锅炉给水BM Boiler Master 锅炉主控BMCR Boiler Maximum Continuous Rating 锅炉最大连续出力BFBP Boiler Feed Booster Pump 锅炉给水增压泵BNR Burner 燃烧器BOP Balance Of Plant 电厂辅机设备BPC Blade Pitch Control 叶片带距控制BT Boiler Tube 炉管CH Crusher House 碎煤房COMB Combustion 燃烧COMP Compressed Air 压缩空气CONV Conveyer 输送机CPL Control Panel Local 就地控制盘CPM Control Panel Main 主控盘CRT Cathode Ray Tube 屏幕显示CT Current Transformer 变流器CYCL Cyclone 旋风分离器CAS Casing 缸CB Cut Breaker 开关COMP Complete 完成CCCW Closed Circulating Cooling Water 闭式循环冷却水CCW Closed Cooling Water 闭式冷却水CCWHF Closed Cooling Water Heater 闭式冷却水冷却器CCWP Closed Cooling Water-pump 闭式冷却水泵CS Closed Cooling Water System 闭式冷却水系统CH Coal Handling 煤的装卸CHK VLV Check Valve 逆止阀CIRC Circulation 循环CLR Cooler 冷却器CLSD Closed 闭式CLOW Cooling Water 冷却水CMPR Compressor 压缩机CNDNR Conditioner 调节器CNTL Control 控制CNTLE Controller 控制器COND Condensate 凝结水CONDTY Conductivity 导电率CP Condensate Pump 凝结泵CIR Circuit 回路COUPI Coupling 藕合，连接CP Condensate Polisher 除盐装置CS Control Switch 控制开关CRSV Cold Reheat Safety Valve 再热器冷段安全阀CV Control Valve 控制阀CWP Circulation Water Pump 循环水泵DMPR Damper 挡板DP Difference Pressure 差压DPIC Differential Pressure Indicating Controller 压差指示控制器DPT Differential Pressure Transmitter 压差变速器DRN Drain 疏水DV Drain Valve 疏水阀DC Direct Current 直流电DSH De-super-heater 减温器DCA Drain Cooler Approach 疏水冷却器通道DEAER De-aerator 除氧器DEV Deviation 偏差DIFFRLY Differential Relay 差动继电器DISCH VLV Discharge Valve 排放阀DIST Disturbance 故障DSCH Discharge 排出ECON Economizer 省煤器EP Electrical Static Precipitator 电除尘ECC Eccentric 偏心EFF Efficiency 效率EHC Electric Hydraulic Control 电液控制EO Electric Operate 电气操作EQ Equipment 设备ER Error 误差ES Extraction System 抽气ESC Escape 逃逸ESS Engineering Safety System 保安系统EU Engineering Unit 工程单位EXH Exhaust 排汽EXT Extract 抽出F Fly Ash System 飞灰系统FA Fine Ash 细灰FDR Feeder 给料机FE Flow Element 流量元件FI Flow Indicator 流量指示件FDBK Feedback 反馈FITG Fitting 连接件FLW Flow 流量FO Fail Open 故障时自动开关FT Flow Totalize 流量累加器FT Flow transmitter 流量变送器FV Flow Control Valve 流量控制阀FY Flow Relay or Valve 流量传送器FA Failure Alarm 故障报警FD Forced Draft 强制通风FDF Forced Draft Fan 送风机FDR Feeder 给煤机FIC Flow Indicate Controller 流量指示控制器FLT Flash Tank 扩容箱FLD Field 磁场FLG Flange 法兰FLM Flame 火焰FWH Feed Water Heater 给水加热器FO Fuel Oil 燃油FREQ Frequency 频率FURN Furnace 炉膛FV Flow Control Valve 流量控制阀GLD Gland 密封GRDR Grinder 碎渣机GND Ground 接地GC Generator Cooling 发电机冷却GEN Generator 发电机GESE Gland Steam Condenser Exhauster 轴封抽汽机GMT Generator Main Transformer 发电机变压器GRAD Grandient 梯度GS Gland Steam 轴封蒸汽GSC Gland Steam Condenser 轴封加热器GV Governor Valve 压调门H Heat Conservation 保温HO Heavy Oil 重油HP High Pressure Horse Power 高压马力HS Hand Switch 手动开关HTR Heater 加热器HV Hand Control Valve 手动控制器HY Hand Relay or Transducer 手动继电器（转换器）H Hand 手动的HB Heat Balance 热平衡HD Heater Drain 加热器疏水HD der 联箱HL Heat Loss 热损失HMDY Humidity 湿度HPH High Pressure Heater 压加热器HPR Hooper 漏斗HPT High Pressure Turbine 高压缸HR Hot Reheat 再热器，热段HR Heat Rate 热耗率HSV Hot Reheat Safety Valve 再热器热段安全阀HT Heat 加热HTG Heating 加热HTR Heater 加热器HVAC Heating Ventilation & Air Conditioner 加热通风与空气调节HW Hot-well 热井HV Hand Control Valve 手动控制器HYD Hydraulic 液力的INTLK Interlock 联锁IC Instrument and Control 仪表与控制（热工）ICV Intermediate Control Valve 中压控制阀ID Induced Draft 抽风，引风IDF Induced Draft Fan 引风机IGN Ignition 点火装置INLT Inlet 入口IPR Initial Pressure 初压INST Instrument 仪表INVR Inverter 倒相器，转换开关I /O Input/Output 输入/输出IP Intermediate Pressure 中压IPT Intermediate Pressure Turbine 中压缸ISV Intermediate Pressure Turbine Steam Valve中压缸，进汽阀JP Jet Pump 喷射器LG Level Gauge 料位计LUB Lubricate 润滑油LVL Level 水位，液位LA Level Alarm 液体报警LIM(LMIR) Limiter 限制器LKG Leakage 泄漏LP Low Pressure 低压L.P Low Point 低位LPH Low Pressure Heater 低压加热器LS Live Steam 主蒸汽LSH Local Switch Hand 就地开关LUB OIL Lube Oil 润滑油M Mechanical 机械Motor 马达MAG Magnetic 磁性MOD Mode 方式M/A Manual/Automatic 手动/自动MAN Manual 手动MARG Margin 极限MAX Maximum 最大的，最大值的MCR Maximum Continuous Rating最大连续出力MCV Main Control Valve 主控制阀MD Modulation Damper 调节挡板MDBFP Motor Driven Boiler Feed-water Pump 电动给水泵MEAS Measure 测量MFT Master Fuel Trip 主燃料切断MIN Minimal 最小的MKUP (MU) Make-up 补充ML Mill 磨煤机MN Main 主要的M.O. Manual Operate 手操MPT Main Power Transformer 主变压器MS Main Steam 主蒸汽MSV Main Steam Valve 主汽阀NOZ Nozzle 喷嘴NPSH Net Pump Suction Heat 泵的静吸压头OL Overload 过载OLR Overload Relay 过载继电器OPER Operation 运行OSC Oscillograph 示波器OTLT Outlet 出口PA Primary Air 一次风PAF Primary Air Fan 一次风机PAH Pressure Alarm High 高压报警PAL Pressure Alarm低压报警PAS TDBFP A Status 汽动给水泵A状态PB Push Button 按钮PBS TDBFP B Status 汽动给水泵B状态PC Power Center 动力中心PC Pressure Controller 压力控制器P.C. Pressure Control 压力控制PCP Precipitator 除尘器PCV Pressure Control Valve 压力控制阀PDI Pressure Differential Indication 差压指示计PDT Pressure Differential Transmitter 差压变送器PED Pdestal 轴承座PERF CALC Performance Calculation 性能计算PF Power Factor 功率因数PHTR Pre-heater 预热器PMP Pump 泵PNEU Pneumatic 气动的PR Pressure Recorder 压力记录计PRG Purge 吹扫PRV Pressure Relief Valve 泄压阀PRO Protection 保护PROGR Program 程序PT Pressure Transmitter 压力变送器PULV pulverizer 磨煤机PVSV Pressure Vacuum Safety Valve压力真空安全阀PW Plant Water 厂用水PY Pressure Relay 压力继电器QA Quality 质量，性能RB Run Back 快速降负荷RCV Recovering 回收RCV Reverse Current Valve 逆止阀RECIRC Re-circulation 再循环RECT Rectifier 整流器RED Reducer 减压器RET Return 返回RH Re-heater 再热器RO Restriction Orifice 节流孔板ROT Rotor 转子RTU Remote Telemetry Unit 遥测装置SA Secondary Air 二次风SAT Saturate 饱和的SC Steam Coil Air Heater 暖风器SCAV Scavenge 吹扫SCN Scanner 控制器SD Shut-off Damper 关断挡板Shut-Down 停止运行SEP Separator 分离器SG Switchgear 开关装置SH-DN Shut-Down 切除SH Super-heater 过热器SLS Seals 密封SO Shut Off 关闭SPD Speed 转速SPRA Spray 喷水SPT Support 支持，支架ST Start 启动，开始STD-BY Stand By 备用ST System 系统STM Steam 蒸汽STR Stator 定子STRNR Strainer 滤器SU Start Up 启动SV Solenoid Valve 电磁阀Shut Off Valve 关断阀SUCT Suction 吸入SW Switch 开关Steam Water 汽水SBLWR Soot Blower 吹灰器TBFP Turbine Drive Boiler Feed-water Pump 汽动给水泵TCV Temperature Control Valve 温度控制T.B. Transfer Damper 转换挡板TE Temperature Element 测量元件TG Turbine-generator 汽轮发电机Turbine-gear 汽机盘车THERM Thermal 热力的TMS Turbine Master System 汽机主控TRANS Transfer 转换TRBL Trouble 故障TRKG Tracking 跟踪TRX TURBOMAX 汽机最大热应力控制TT Temperature Transmitter 温度传感器TTD Terminal Temperature Difference 温度端差TURB Turbine 汽机TW Thermo-well 热电偶套管UAM Unit Automatic Master 机组自动系统VAC Vacuum 真空VAL Value 数值VB Vibration 振动VLV Valve 阀门WH Watt-hour 瓦小时WP Work Point 工作点WW Water Wall 水冷壁WX Watt Transducer 功率转换器COVER Crossover 切换管CV Control Valve 控制阀PS Position Switch 状态开关，位置开关PT Position Transmitter 状态变送器BOOSTER PUMP FREE SIDE BEARING TEMP前置泵自由端径向轴承温度BOOSTER PUMP DRIVEN SIDE BEARING TEMP前置泵驱动端径向轴承温度BOOSTER PUMP THRUST BEARING OUTSIDE TEMP前置泵推力轴承外侧温度BOOSTER PUMP THRUST BEARING INSIDE TEMP前置泵推力轴承内侧温度comment 注释，评论module 模块standby 备用proximity 相近，接近，亲近detector 探测器bracket 支架interlocks 互锁，连锁axial 轴向的surge conditions 喘振loss of speed 飞车accessory 附件pulsation 有节奏的跳动，跳动fossil fired 燃煤intent 意图，目的，意向intend 意指，想要，打算consistent 一致的，调和的practice 惯例，实习，实践intrinsic 固有的，内在的procurement 获得，获取fabrication 制作，构成，伪造物vent 通风孔，出烟孔，出口，放出，排出，发泄noncondensible gas 不凝结气体intermittent 间歇的，断断续续的blowdown 排污tank 桶，箱，罐diagram 图表deaerator 除氧器corrosion 侵蚀，腐蚀状态concentration 集中，集合，浓缩，浓度recommend 推荐，介绍，托付，劝告abnormal and normal conditions 变工况和额定工况warm up 暖机acid wash 酸洗scale 范围，水垢，水锈，比例，刻度sludge 污泥，淤泥foreign matter 不相关的物质facilitate 推动，促进，使简化multistage 多级的remote control 遥控safety relief valve 安全卸压阀gauge 量规，量表，测量manhole 人孔，检修孔equivalent 等价物，相等的forging 锻造seat 部位，座socket welding 管座焊接enthalpy 焓estimate 评价，评估，估价parameters 参数，参量nominal 名义上的，额定的，标称的MS—Main Steam 主蒸汽Cycle循环Intercept截止Fetting附件Gage规，表，压力计Taps接头test wells测点插孔stress-relieved 应力消除thermometer温度计steam purge system蒸汽吹扫系统centrifugal type pumps离心式泵margin余量friction losses磨擦损失solenoid螺线管modulat调整，调节criteria标准wrenches扳手pipe taps管接头Assemble 集合，集结，组装Group 聚合，成群Vibration 振动audio 声频的，音频的integral 部分，完整，积分，完整的boiler house 锅炉房coal conveyor 输煤装置coal bunker 煤仓coal mill 磨煤机steam boiler water boiler tube蒸汽锅炉，管式锅炉furnace(combustion chamber) 炉膛(燃烧室) water tube 水管ash pit 灰坑super-heater 过热器water pre-heater 水预热器air pre-heater 空气预热器gas duct(flue) 烟气管,烟道dust collecting plant 集尘室electrical precipitation plant 电气除尘室induced draught fan 引风机chimney 烟囱de-aerator 除氧器feed water tank 供水箱boiler feed pump 给水泵switchgear 开关设备cable tunnel 电缆通道cable cellar 电缆槽turbine room 汽轮机室steam turbine with alternator蒸汽汽轮发电机组economizer 省煤器steam drum 汽包surface condenser 表面凝汽low-pressure pre-heater 低压预热器circulating water pipe(pump) 循环水管control room 控制室electrostatic dust remover(precipitator)静电除尘器pulverizer 磨煤机slag pump 灰渣泵thermal cycle 热力循环(net)heat rate （净）热耗率STEAM POWER STATION 火力发电站。

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。

燃煤锅炉的燃烧进程控制大学毕业论文外文文献翻译及原文

毕业设计（论文）外文文献翻译文献、资料中文题目：燃煤锅炉的燃烧进程控制文献、资料英文题目：Controlling the Furnace Process in Coal-Fired Boilers文献、资料来源：文献、资料发表（出版）日期：院（部）：专业：班级：姓名：学号：指导教师：翻译日期： 2017.02.14Controlling 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 of loads, minimize heat losses, reduce the extent to which the furnace is contaminatedwith 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 quantitative parameters of which can be estimated only indirectly or by special measurements. Thequality 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 first model is for the case when jets flow into a ―free‖ space (G1= 0),the second model isfor 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 the 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 or lower the flame, but also to concentrate or disperse the release of heat in it [1]. A verytangible 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 combustion (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 and four) placed in a tier (on one side of the furnace). The furnaces have the same totaloutlet 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 f urnace: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 fuel and 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 furnace device is given in [2]. As for boilers of larger capacity, work on developingcontrollable 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.。

锅炉系统毕业设计论文中英文资料对照外文翻译文献

中英文资料对照外文翻译文献锅炉系统1 冷凝器1.1 简介欧堡生产的冷凝器是用直管和一个外部密封浮头组成的管壳式冷凝器。

这种冷凝器主要用作废气锅炉，蒸汽加热或洗舱海水加热器的转储冷凝器/冷却器排水。

并取得权威船级社批准。

温度计，排水阀，空气阀，压力表的安装设计为½“BSP内螺纹安装。

这些组件可能是指定的。

而蒸汽或水的控制设备是可选的。

1.2 安装空间要求安装时必须有足够的空间供作清洗，检查或更换管的插入与撤出。

冷凝器必须安置在水平并稳定的表面。

1.3 存储如果冷凝器在安装前要闲置一段时间，应存放在干燥的储藏室里。

如果储藏室潮湿，冷凝器必须放在装有硅胶的包装袋子里。

为了避免破坏，建议冷凝器放在原包装中。

冷凝器已经在交付前做过液压试验。

试验中所用测试媒质含有一定的数额抗腐蚀保护物质。

当冷凝器需闲置的时间较长，建议使用指定产品作为防腐蚀物质1.4 安装冷凝器设计为垂直或水平安装。

在水平安装的情况下，蒸汽喷嘴必须朝上，而冷凝水出口喷嘴朝下。

如果是垂直安装冷凝器，蒸汽入口和海水出口端必须朝上。

排水和空气排放阀必须安装在冷凝器在最低和最高点的中间线的位置。

任何选择性的控制设备必须根据具体指示安装。

步骤A：将冷凝器安装在水平平面上。

步骤B：钻基础固定螺栓孔。

步骤C：将螺栓放入孔中并拧紧。

连接冷凝器步骤D：移除所有的塞子和盲板，然后再连接冷凝器。

步骤E：在连接中确保没有杂质进入。

步骤F：管道连接起来，确保从管道和冷凝器之间没有强制力的产生。

1.5 调试启动前要确保所有连接都牢固地拧紧是很重要的。

同样重要的是，冷凝器和连接管道空气要彻底排出。

步骤A：如果装有安全阀，必须加以调整到最大设计压力或较低。

步骤B：法兰螺栓要拧紧。

拧紧法兰螺栓时始终使用扭矩扳手。

步骤C：运行一小时，停止冷凝器，并重新拧紧所有螺栓。

步骤D：启动阶段，冷凝器的两边都要排出空气，必须认真仔细的检查回路的泄漏。

1.6 性能冷凝器性能须附和传热计算表规定的要求。

锅炉专业英语中英文对照表(综合版)

boiler锅炉boiler unit锅炉机组stationary boiler固定式锅炉steam boiler/generator蒸汽锅炉utility boiler电站锅炉industrial boiler工业锅炉hot water boiler热水锅炉indoor boiler室内锅炉ourdoor boiler露天锅炉package boiler快装锅炉shop-assembled boiler组装锅炉field-assembled boilerfield-erected boilersupercritical pressure boiler超临界压力锅炉subcritical pressure boiler亚临界压力锅炉superhigh pressure boiler超高压锅炉high pressure boiler高压锅炉medium pressure boiler中压锅炉low pressure boiler低压锅炉natural circulation boiler自然循环锅炉forced circulation boiler强制循环锅炉assisted circulation boiler辅助循环锅炉controlled circulation boiler控制循环锅炉once-through boiler直流锅炉combined circulation boiler复合循环锅炉low circulation-ratio boiler低循环倍率锅炉solid-fuel fired boiler固体燃料锅炉liquid-fuel fired boiler液体燃料锅炉coal fired boiler燃煤锅炉oil fired boiler燃油锅炉gas fired boiler燃气锅炉multi-fuel fired boiler混烧锅炉boiler with dry-ash furnaceboiler with dry-bottom furnaceboiler with slag-tap furnaceboiler with wet-bottom furnacesupercharged boiler增压锅炉water tube boiler水管锅炉cross drum boiler横锅筒（汽包）锅炉longitudinal drum boiler纵锅筒（汽包）锅炉shell boiler锅壳锅炉horizontal boiler卧式锅壳锅炉vertical boiler立式锅炉stationary boiler of locomotive type固定式机车锅炉π-type boiler （two-pass boiler)π型锅炉box-type boiler箱型锅炉tower boiler 塔型锅炉散装锅炉固态排渣锅炉液态排渣锅炉D-type boilerD 型锅炉rated capacitynominal capacitymaximum continuous rating最大连续蒸发量rated heating capacity额定供热量nominal steam conditionnominal steam parameternominal steam pressure额定蒸汽压力nominal steam temperature额定蒸汽温度(nominal) hot water temperature热水温度feed water temperature给水温度return water temperature回水温度circulation circuitsteam generating circuitsteam purification蒸汽净化steam temperature control汽温调节feed water给水condensate凝结水make-up water补给水boiler water锅水；炉水boiling crisis沸腾换热恶化as-fired fuel炉前燃料fire bedfuel bedfire line最高火界additive添加剂flue gas dew point烟气露点boiler circulation水循环mechanical carry-overmoisture carry-overvaporous carry-over溶解携带water separation汽水分离steam washing蒸汽清洗stage evaporation分段蒸发pressurized firing压力燃烧negative-pressure firing负压燃烧grate firing火床燃烧suspension firing火室燃烧；悬浮燃烧tangential firing切向燃烧opposed firing对冲燃烧cyclone-furnace firing旋风燃烧fluidized-bed combustion沸腾燃烧gas recirculation烟气再循环natural draft自然通风mechanical draft机械通风balanced draft平衡通风forced draft 正压通风火床机械携带额定蒸发量额定蒸汽参数循环回路induced draft负压通风zone control分段送风pressure atomizationmechanical atomizationtwin-fluid atomization双流体雾化rotary-cup atomization旋杯雾化；转杯雾化direct leakageinfiltration leakagebypass leakageentrained leakageboiler proper锅炉本体heating surface受热面radiant heating surface辐射受热面convection heating surface对流受热面pressure part受压部件；受压元件cylindrical shell筒体head封头；端盖header集箱；联箱tube panel管屏up flow riser tube panel垂直上升管屏ribbon panel回带管屏spirally-wound tubes水平围绕管圈tube bundle管束gas passgas ductconvection pass对流烟道parallel gas passes并联烟道air duct风道arch拱furnace arch折焰角water-cooled hopper bottom冷灰斗wall with refractory liningrefractory beltsupporting tube悬吊管design pressure设计压力maximum allowable working pressure最高允许工作压力maximum allowable metal temperature最高许用壁温furnace enclosure design pressure炉膛设计压力heat input输入热量heat output锅炉有效利用热量fuel consumption燃料消耗量calculated fuel consumption计算燃料消耗量ash-retention efficiency排渣率load range at constant temperature（保持）额定汽温的负荷范围injection flow(rate)喷水量blowdown flow(rate)排污量theoretical air 理论空气量卫燃带压力雾化；机械雾化直接泄漏间接泄漏烟道excess air ratio过量空气系数hot air temperature热风温度exhaust gas temperature排烟温度theoretical combustion temperatureadiabatic temperaturefurnace outlet gas temperaturefurnace exit gas temperaturepressure drop汽水阻力draft losspressure dropstack draft自生通风压头available static head运动压头circulation ratio循环倍率circulation velocity循环水速steam quality by mass质量含汽率；干度mass velocity质量流速critical steam quality临界含汽率steam quality at minimum heat transfercoefficient最高壁温处含汽率furnace volume炉膛容积furnace volume heat release rateheat liberation rate in furnacefurnace cross-section heat release ratefurnace plan heat release rateburner zone wall heat release rate燃烧器区域炉壁热负荷furnace wall heat release rate炉壁热负荷furnace wall heat flux density炉壁热流密度critical heat flux density临界热流密度grate heat release rate炉排（面积）热负荷burner heat input燃烧器热功率ignition energy点火能量evaporation rate受热面蒸发率percentage of economizer evaporation省煤器沸腾率primary air一次风secondary air二次风tertiary air三次风imaginary circle假想切圆percentage of air space通风截面比fineness煤粉细度explosion mixture limits爆炸界限furnace炉膛；炉胆fire box火箱smoke box烟箱burner燃烧器tilting burner摆动式燃烧器igniter点火器oil atomizer 油雾化器理论燃烧温度炉膛出口烟气温度通风阻力炉膛容积热负荷炉膛截面积热负荷register调风器stabilizer稳燃器wind box风箱burner portburner quarlgrate炉排hand-fired grate手烧炉排stoker-fired gratemechanical stokertravelling grate stoker链条炉排chain grate stoker链带式炉排bar grate stoker横梁式炉排louvre stoker鳞片式炉排vibrating stoker振动炉排inclined reciprocating grate往复炉排spreader stoker抛煤机air compartment风室reinjection system飞灰复燃装置drum锅筒；汽包steam drum上锅筒water drum下锅筒shell锅壳drum internals锅筒内部装置；汽包内部装置steam washer清洗装置cyclone separator旋风分离器turbo separator轴流式分离器baffle plate缝隙挡板corrugated scrubber百叶窗分离器screen separator钢丝网分离器perforated distribution plate多孔板dry pipe集汽管evaporating heating surface蒸发受热面water-cooled wall水冷壁membrane wall膜式水冷壁division wall双面水冷壁anti-clinker box防焦箱gererating tube bankboiler convection tube bankboiler (slag) screen防渣管fire tube ；smoke tube烟管；火管mixer混合器superheater过热器radiant superheater辐射过热器wall superheater墙式过热器platen superheater屏式过热器convection surperheater对流过热器steam-cooled wall 包墙过热器燃烧器喷口机械炉排锅炉管束steam-cooled roof顶棚管过热器reheater再热器attemperatordesuperheatersurface type attemperatorsurface type desuperheaterspray type attemperatorspray type desuperheaterbifluxreheater superheater attemperatorbypass damper旁路挡板economizer省煤器steaming economizer沸腾式省煤器steel tube economizer钢管省煤器finned tube economizer鳍片管省煤器cast-iron gilled tube economizer铸铁省煤器air heater空气预热器tubular air heater管式空气预热器rotary air heaterregenerative air heater rotating-plate type regenerativeair heaterLjungstrom type air heaterstationary-plate type regenerativeair heaterrothemuhle type air heatersteam air heater暖风器boiler structure锅炉构架top-supported structure by beams支承式锅炉构架top-supported structure by hangers悬吊式锅炉构架buckstay刚性梁inner casing内护板outer casing外护板boiler steam and water circuit锅炉汽水系统boiler external piping锅炉范围内管道start-up system启动系统start-up flash tank启动分离器safety valve安全阀safety relief valve安全泄放阀water level indicator水位表injector注水器boiler setting炉墙soot blower吹灰器slag removal equipment除渣设备boiler efficiency锅炉效率；锅炉热效率boiler operating availability锅炉可用率boiler forced outage rate锅炉事故率feed water condition 给水品质汽-汽热交换器回转式空气预热器受热面回转式预热器风罩回转式预热器减温器面式减温器喷水减温器steam purity 蒸汽品质moisture in steam 蒸汽湿度boiler water concentration 锅水浓度；炉水浓度total dissolved salt 总含盐量total solid (matter)全固形物dissolved solid (matter)溶解固形物suspended solid (matter)悬浮物total hardness （总）硬度alkalinity 碱度heat loss 热损失heat loss due to exhaust gas 排烟热损失heat loss due to unburned gases 气体（化学）未完全燃烧热损失heat loss due to unburned carbon inrefuse 固体（机械）未完全燃烧热损失heat loss due to radiation 散热损失heat loss due to sensible heat in slag 灰渣物理热损失unburned combustible in flue dustunburned carbon in flue dust unburned combustible in slagunburned carbon in slag unburned combustible in sifting 漏煤可燃物含量dust loadingdust density load range of boiler 锅炉负荷调节范围turndown ratio 燃烧器调节比air leakage factor 漏风系数set pressure 整定压力start-to-discharge pressure 前泄压力popping pressure 起座压力reseating pressure 回座压力blowdown 回座压差discharge capacity 排放量；排汽能力boiler efficiency test 锅炉效率试验；锅炉热效率试验hydrostatic test 水压试验hydrostatic deformation test 验证性水压试验air leakage test 漏风试验pressure decay test 风压试验load test 负荷试验circulation test 水循环试验thermal chemical test 热化学试验sounding of tube by balls 通球试验safety valve operating test 安全阀校验flue gas analysis 烟气分析Orsat (gas analyser)奥氏（烟气）分析器suction pyrometer 抽气式热电偶（高温计）venturi pneumatic pyrometer 气力式高温计heat flux meter 热流计飞灰可燃物含量；飞灰含碳量炉渣可燃物含量；炉渣含碳量烟气含尘量start-up启动filling上水water level水位initial water level点火水位purge吹扫blowoff放水drain疏水blowdown排污raising pressure升压bringing a boiler onto the line 并汽start-up pressure启动压力start-up flow rate启动流量shutdownoutageout of service停用banking fire压火storage停炉保护chemical cleaning化学清洗boiling-out（碱）煮炉flushing冲管steam-line blowing 吹管passivating钝化drying-out烘炉flow stagnation停滞flow reversal倒流separation of two-phase fluid 汽水分层steam bindingsteam blanketingpriming汽水共腾foaming泡沫共腾external deposit烟气侧沉积物internal deposit汽水侧沉积物slagging结渣fouling积灰clogging堵灰pitting attack点状腐蚀ductile gouging延性腐蚀hydrogen damage 氢脆caustic embrittlement苛性脆化high temperature corrosion 高温腐蚀low temperature corrosion 低温腐蚀overheating超温；过热flashback回火blow off脱火loss of ignition熄火；灭火furnace explosion炉膛爆炸furnace implosion 炉膛内爆汽塞停炉furnace puff炉膛爆燃blow hole火口secondary combustion二次燃烧。

工业锅炉节能毕业论文中英文资料外文翻译文献

工业锅炉节能中英文资料外文翻译文献专业英文资料Boiler energy savingIndustrial boiler energy saving technology related to many, what is the most important increase industrial furnace thermal utilization ratio of pot namely, increasing the thermal efficiency of the industrial boiler. This section from burning, transportation line maintenance, new technology and new equipment and the application of the industrial boiler auxiliary equipment of energy saving, pot boiler water processing, etc and the industrial boiler room way of energy saving is discussed in this paper.1. The furnace of industrial boiler furnace arch arch is very important. The role is to make arch furnace chamber of the mixture of gases and radiation and hot gas organization flow, to make the fuel and ignition and combustion when. Sua and at present industrial boiler with the actual YongQiLiang rated load are often not with horse, the use of coal changes greatly, and often have large design coal poor vision, so in actual use, often to furnace necessary improvement in arch coal need to be comfortable.For transformation of the former furnace arch situation, the existing problem is: for the use of coal and coal than design poor miscellaneous, boiler flue gas temperature appear the chamber exports low (about 700℃), more than 200 ℃ design low. The new coal fire late, often appear fire bed broken fire, fire from about 0.6 ~ coal disc 1 cm, furnace combustion is not strong, ash high carbon content. According to the problems furnace arch structure, from improving the ignition of fuel conditions and raise the temperature of boiler furnace to reform.After improvement furnace arch, in actual shipped in from the observed, the transformation effect is good, people away from coal furnace fuel after disc 0.3 MRP on fire, fire bed combustion intense, flame full of degree good, strong rotation. Due to the lower arch before, after extended arch, the arch of the throat and mouth shape between into space from the original 2 cm or so down to 1 cm. To strengthen the disturbance of the air mixed, to form the airflow, strengthen the furnace combustion, improve the efficiency of the district and the whole arch before furnace temperature, make its reach to 1400℃ above, improved the ignition of fuel conditions. Coal in the ignition, of furnace temperature rise, make the carbon content and ash significantly less. The flue gas mixture and strengthen the hydrocyclone separation of flue gas carbon particles needed to fall in the fire bed and new fuel layer further burns out.2. The reasonable air supply and regulationIn the chain furnace, the furnace, the furnace of reciprocating vibration, according to the different characteristics of the combustion process, reasonable air supply, to promote the furnace combustion is very important. As in the chain furnace, along with fuel keep movement, which in turn happen on fire, burning, and burn the stage. Burning along the length direction is the stoker stages, zoning, so along the length direction along the air quantity is also different. The preheating zone along the head and tail burn stage, air requirements small; The burning along the middle stage, air requirements. According to this13characteristic, must use block supply air, to meet the needs of the burning. The current domestic production of the boiler although all are to consider this one characteristic, with the wind in subsection room, and equipped with air inlet adjustment. But according to the survey.3.The secondary airSecond wind to strengthen the air combustion is very effective. Second wind have the following function:(1) strengthen the furnace of air disturbance and mixed, make the furnace of oxygen and flammable gas mixture evenly, make chemical don't fully burning loss and the chamber excess air coefficient reducing. (2) secondary air in furnace flue gas vortex formed, on the one hand, extended the suspension fine coal grain in the chamber of a stroke, increase the fine particles suspended furnace in the residence time of, make it have a full time to burn, make not complete combustion heat loss; Another result of air separation of spiral effect, make coal dust grain and the grain re-blows rejection within, and reduce the small fly ash escape from the quantity, the mechanical incomplete combustion heat loss.英译汉14锅炉的节能工业锅炉的节能技术涉及多方面 , 最主要是提高工业锅炉的热能利用率 , 即提高工业锅炉的热效率。

燃煤锅炉外文翻译外文文献英文文献中英翻译

燃煤锅炉外文翻译外文文献英文文献中英翻译外文出处: A. A. Shatil’, N. S. K. A. A. S., & V. Kudryavtsev, A. (2008). Controllingthe furnace process in coal-fired boilers. Thermal Engineering, 55, 1, 72-77.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 ofcontrolling 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 calculationstudies.The experience Central Boiler-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 andmaneuverable—in other words, controllable—furnace devices that had been put in operationat 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 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 offuel 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 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 making use of the following three main factors:(i) the flows of oxidizer and gases being set to move in the flamein a desired aerodynamic manner;1(ii) the method used to supply fuel into the furnace and the placeat 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 withthe 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 bysetting up bulky vortices transferring large volumes of air and combustion products across and along the furnace device. If fuel isfired 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 especially typical of highly intense furnace devices. The combustion process in the se 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 theemission of nitrogen oxides .Also important for the control of a furnace process when solid fuelis 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 Vdaf < 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 quantitative parameters 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 turbulized at the outlet from a nozzle or burner, the shorter the distance which it covers, and, accordingly, the less completely the components are mixed in2the 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 way Where ks is a proportionality factor tha t depends on the ―pitch‖ between the jet axes (ks=1.5–1.8).The results of an experimental investigation inwhich 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 flowrate G2 that enter into a stream with flowrate G1. The first model is for the case when 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 the third model is for the case ,when jets flow into a drift stream with flowrate G1<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 initialsection can be determined using the well-known empirical formula of G.N. Abramovich [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 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?20. This value is close to the actual values found in furnacesequipped with once through burners. In furnaces equipped with swirl burners, a= 0.14 and Ff/Fb?10. In both cases, the interval between theburners is equal to the jet diameter in the transition section d tr , which differs little from the value that has been established inpractice and recommended in [7].3The method traditionally used to control the furnace process inlarge 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 themaffect the entire process only slightly. A furnace design employinglarge 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 or lower the flame, but also to concentrate or disperse the release of heat in it [1].A very tangible effect 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, 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 flowrate ofair through them, their equivalent diameters deq will become smaller, as willthe jet momentums Gbwb, 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 whenthe emissions of NOx and CO are suppressed right inside the furnaceusing staged combustion (at αb < 1) under the conditionsof a fortiori 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 chambers4differing in the number of once through round nozzles (two and four) placed in a tier (on one side of the furnace). The furnaces have the same total outlet cross-sectional areas of the nozzles (ΣFb) 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 entersthrough once through burners into the furnace volume beneath themcan be estimated using the formula βair = 1 – (3) which has been verified in the range = 0.03–0.06 for a furnacechamber 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 raction βair will decreas e from 0.75 to 0.65. Thus, Eq. (3) may be written in the following fform 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 furnacedepth af (at the same = idem) using the expression (5)It should be noted that the axes of two large opposite air nozzles ( = 1)—an arrangementimplemented 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 throughjets 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 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 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 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 fuel and air nozzles spaced apart from one another over the furnace perimeter, accompanied 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 ofwhich are arranged transversely with respect to the main direction of gas flow have wide possibilities in terms of5controlling 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 frontusing a highconcentration dust system, showed that the temperatureof gases at the outlet from the furnace had a fairly uniformdistribution 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 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 with steam capacities ranging from 50 to 1650 t/h with such anaerodynamic 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 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 acceptancein 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 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 (thetransliterated 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 inthe 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 flowrate and6fractions. The design of one such device is schematically shown in [9]. Figure shows a distribution of fuel flowrates 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.7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。

锅炉烟气除尘系统设计环境工程外文资料翻译

毕业论文外文资料翻译题目某燃煤采暖锅炉烟气除尘系统设计学院资源与环境学院专业环境工程班级学生学号指导教师张玲二〇一二年四月二十日济南大学- 1 -济南大学- 2 -济南大学- 3 -济南大学- 4 -- 5 -济南大学- 6 -济南大学- 7 -济南大学- 8 -济南大学- 9 -济南大学- 10 -济南大学Chemical Engineering and Processing 40 (2001) 245–254.新的旋风式分离器的计算方法与纷飞挡板和底部清洁的天然气 - 第二部分：实验验证Tomasz Chmielniak a,*, Andrzej Bryczkowskia,b煤化工Zamkowa1，41-803 Zabrze，波兰研究所化学和工艺设备，波兰西里西亚技术Uni6ersity，M. Strzody7，44-100格利维采1999年11月23日收到，在2000年6月6日修订后的形式;2000年6月6日采纳摘要派生模型预测研究所收集的效率和压力下降，煤化工（IChPW）与一个旋转挡板的旋风式分离器的设计测试和实验验证的结果。

试点工作包含测试气体流速和分离效率和压降转子转速的影响。

密封流除尘效率的影响进行了测试。

一个旋转挡板分隔的特点是高效率和低的压降。

挡板高度的扩展可以得到较高的除尘效率和更低的压降。

计算方法与实验结果显示了良好的实验预期。

关键词粉尘分离；气旋；旋流挡板；收集效率；压降1介绍由于旋转分离元素的粉尘分离器的优势，致使过去几年对这类设备[1-5]建设的深入研究和理论描述。

它还涉及建设一个在化工、煤炭加工（IChPW）研究所开发的新型旋风式分离器旋流挡板[6]。

在这个问题上[6]前文推导的理论模型来预测一个旋转挡板分离器的收集效率和压力下降。

在本文章中，发达国家的计算方法的实验和实证检验的结果报告。

2 旋风式分离器的计算方法的理论与旋流挡板2.1收集效率级效率的模型来预测的基础上的Laith和利希特气旋的计算方法[7]。

【精品】锅炉的计算机控制外文翻译外文文献英文文献

【关键字】精品英文翻译Boiler computer controlBoiler computer control：The boiler micro computer control, is a new technology which the recent years developed, it was the microcomputer soft, the hardware, the automatic control, the boiler energy conservation and soon several technical in close integration with product, our country existing center, small boiler more than 300,000, the coal consumption accounted for our country raw coal output every year 1/3, at present the majority industry boiler still was at the energy consumption to be high, to waste, the environmental pollution in a big way and so on the serious production condition. Enhances the thermal efficiency, reduces the coal consumption, carries on the control with the microcomputer is has the profound significance the work. As the boiler control device, its primary mission is guaranteed the boiler the security, is stable, the economical movement, reduces operator's labor intensity. Uses the micro computer control, can carry on the process to the boiler the automatic detection, the automatic control and so on many functions. The boiler microcomputer control system, generally is composed by the below several parts, namely by the boiler main body, a measuring appliance, the microcomputer, the hand automatic cut over operation, the implementing agency and the valve, the slippery difference electrical machinery and so on partially is composed, a measuring appliance the boiler temperature, the pressure, the current capacity, the oxygen quantity, the rotational speed isometric transforms the voltage, the electric current and so on sends in the microcomputer, the hand automatic cut over operation part, manual when by the operator hand control, controls the slippery difference electrical machinery and the valve with the manipulator and so on, is automatic when sends out the control signal to the microcomputer partially to carry on the automatic operation after the execution. The microcomputer carries on the monitor to the entire boiler movement, reports to the police, the control guaranteed the boiler is normal, reliably moves, except for this for guaranteed the boiler movement these curity, when carries on the microcomputer system design, to the boiler water level, the boiler dome pressure and so on the important parameter should establish theconventional measuring appliance and the alarm device, guaranteed the water level and the dome pressure have the dual even tertiary alarm device, this is essential, in order to avoid the boiler has the significant accident.Control system:The boiler is a more complex controlled member, it not only adjustment quantity many, moreover between various types and quantities mutually relates, mutually affects, mutually restricts, boiler interior energy conversion mechanism quite complex, therefore must establish a more ideal mathematical model to the boiler quite to be difficult. Therefore, has made the boiler system simplification processing, decomposes is three relatively independent governing systems. Certainly also may subdivide other system like amount of wind control loops in certain systems, but it mainly is following three parts: (1) the chamber negative pressure (2) the boiler combustion process has three duties for the main tuning quantity special burning regulator system: To coal control, to wind control, chamber negative pressure control. The maintenance coal gas and the air proportion cause the air too much coefficient about 1.08, the combustion process efficiency, the maintenance chamber negative pressure, therefore the boiler combustion process automatic control is a complex question. As for 3×6.5t/h the boiler burning diffuses the blast furnace coal gas, the request is the blast furnace coal gas which maximum limit uses diffuses, therefore may most greatly strive according to the boiler to move, does not make the strict request to the steam pressure; The burning efficiency does not make a higher request. Such boiler combustion process automatic control simplifies as the chamber negative pressure primarily parameter decides the coal gas flow control. (3) the chamber negative pressure Pf size is directed the amount of wind, the drum amount of wind and the coal spirit (pressure)three influences. The chamber negative pressure too is small, the chamber and outside divulges the blast furnace coal gas to the outside to riching, endangers the equipment and the movement personnel's security. The negative pressure too is big, the chamber leaks the amount of wind to increase, discharges fume the loss to increase, drawing fan electricity consumes the increase. Tried to find out according to the many years man-power manual regulation that, 6.5t/hboiler Pf=100Pa carries on the design. The adjustment method is the original state first by the manual regulation air and the coal gas proportion, achieved the ideal burning condition, all opens when the drawing fan achieved chamber negative pressure100Pa, after the investment is automatic, only adjusts the coal gas reed valve, enable under the fluctuation of pressure the blast furnace coal gas current capacity to tend to the original state coal gas current capacity, maintains in burning the blast furnace coal gas and the air proportion achieves the optimum condition.Boiler water-level control unit ：The steam drum water level is affects the boiler safe operation the important parameter, the water level excessively high, can destroy the soft drink disengaging gear the normal work, is serious when can cause the steam including water to increase, increases on the pipe wall the scaling and the influence steam quality. Water level excessively low, then can destroy the water cycle, causes Water Wall bursting, is serious when can create does the pot, damages the steam drum. Therefore its value has outdone lowly all possibly creates the significant accident. It is adjusted the quantity is the steam drum water level, but adjusts the quantity is for the water current capacity, through to gives the water current capacity the adjustment, enables the steam drum interior the material to achieve the dynamical equilibrium, changes in the permission scope, because the boiler steam drum water level assumes the positive character isticto the vapor current capacity and for the fluent quantity changer But when load (vapor current capacity) sharp growth, the performance actually is " Counter response characteristic "Namely so-called " False water level " Creates this reason is because time load increase, causes the dome pressure to drop, causes the steam drum boiling temperature to drop, the water ebullition suddenly intensifies, forms the massive steam bubbles, but makes the water level to raise. The steam drum water monitor system, in the essence is maintains the boiler turnover water volume balance the system. It is by the water level took the water volume balance or not control target, through adjusts the water volume how many to achieve the turnover balance, maintains the steam drum water level in the soft drink separation contact surface biggest steam drum nearby the position line, enhances the boiler the vaporization efficiency, the guarantee production safety. Because the boiler water level system is equipped with Since the balance the ability to control the object, in the movement has the false water level phenomenon, in the practical application may use the water level single impulse, the water level steam quantity double weight and the water level, the steam quantity according to the situation, gives the water volume three impulses the control systems. Eliminates the oxygenpressure and the water-level control: Partially eliminates the oxygen to use the single impulse control plan, single return route PID adjustment.Monitoring management system management system:Above the control system generally completes the control by PLC or other hardware systems below, but must complete the function in on position computer: Real-time accurately examines the boiler the movement parameter: For comprehensively grasps the overall system the movement operating mode, the supervisory system the real-time monitor and the gathering boiler related craft parameter, the electrical parameter, as well as the equipment running status and so on. The system has the rich graph storehouse, through the configuration may the boiler equipment graph together with the related movement parameter demonstration in the picture; In addition, but also can tabulate the parameter or form and so on grouping demonstrates. The generalized analysis promptly sends out the control command: The supervisory system basis monitors the boiler performance data, according to the control strategy which establishes, sends out the control command, adjusts the boiler system equipment the movement, thus guaranteed the boiler is highly effective, the reliable movement.(1) diagnoses the breakdown with to report to the police the management: The host controls the center to be allowed to demonstrate, the management, the transmission boiler movement each kind of alarm, thus causes boiler safe explosion-proof, the safe operation rank big enhancement. At the same time, to the records management which reports to the police may cause the owner regarding boiler movement each kind of question, weakness and so on to know from A to Z. In order to guarantee the boiler systematic security, reliably moves, the supervisory system will act according to the parameter which will monitor to carry on the breakdown diagnosis, once will break down, the supervisory system promptly on the operator screen the visual display alarm spot. Reports to the police the correlation demonstration function to cause the user definition the demonstration picture to relate with each spot, like this, when reports to the police occurs, the operator may immediately visit should report to the police the emergency procedures which detailed information and defers to recommends adopts to carry on processing. (2) historic record movement parameter: The supervisory system real-time database will maintain the boiler movement parameter the historic record, moreover supervisory system also. Is equipped with special reports to the police the event diary, with records reports to the police/the event information and operator's change The historic record data basis operator's request,the system may demonstrate is the spurt value, also may for some period of time in mean value. The historic record data may have the many kinds of display mode, for example display mode and so on curve, specific graph, report form; In addition the historic record data also may by apply take the network as the foundation many kinds of application software. (3) calculates the movement parameter: The boiler movement certain movement parameters cannot directly survey ,like the year movement load, the steam consumption, make up the water volume, the condensed water returns to the quantity, the equipment accumulation running time and so on. The supervisory system has provided the rich standard processing algorithm, according to movement parameter which obtains, Derived quantity calculates these.译文:锅炉的计算机控制锅炉的计算机控制：锅炉微计算机控制，是近年来开发的一项新技术，它是微型计算机软、硬件、自动控制、锅炉节能等几项技术紧密结合的产物，我国现有中、小型锅炉30多万台，每年耗煤量占我国原煤产量的1/3，目前大多数工业锅炉仍处于能耗高、浪费大、环境污染等严重的生产状态。

锅炉设计外文翻译---燃煤锅炉的个案事故研究

附录A英文原文A. Kusiak and A. Burns, Mining Temporal Data: A Coal-Fired Boiler CaseStudy, Proceedings of the 9th International Conference, KES 2005, Melbourne,Australia, September 14-16, 2005, in R. Khosla, R.J. Howlett, L.C. Jain (Eds),Knowledge-Based Intelligent Information and Engineering Systems: V ol. III,LNAI 3683, Springer, Heidelberg, Germany, 2005, pp. 953-958.Mining Temporal Data: A Coal-Fired Boiler CaseStudyAndrew Kusiak and Alex BurnsIntelligent Systems Laboratory, Industrial Engineering3131 SeamansCenter, The University of IowaIowa City, IA52242 – 1527, USAandrew-kusiak@AbstractThis paper presents an approach to control pluggage of a coal-fired boiler.The proposed approach involves statistics, data partitioning, parameter reduction,and data mining. The proposed approach was tested on a 750 MW commercialcoal-fired boiler affected with a fouling problem that leads to boiler pluggagethat causes unscheduled shutdowns. The rare-event detection approachpresented in the paper identified several critical time-based data segments thatare indicative of the ash pluggage.1 IntroductionThe ability to predict and avoid rare events in time series data is achallenge that could be addressed by data mining approaches. Difficulties arise from the fact that often a significant volume of data describes normal conditions and only a small amount of data may be available for rare events. This problem is further exacerbated by the fact that traditional data mining does not account for the time dependency of the temporal data. The approach presented in this paper overcomes these concerns by defining timewindows.The approach presented in this paper is based on the two main concepts. The first is that the decision-tree data-mining algorithm captures the subtle parameter relationships that cause the rare event to occur [1]. The second concept is that partitioning the data using time windows provides the ability to capture and describe sequences of events that may cause the rare failure.2 Event Detection ProcedureIn the case study discussed in the next section rare events can be detected by applying the five step procedure. These five steps include:Step 1: Parameter CategorizationThe parameter list is divided into two categories, response parameters and impact parameters. Response parameters are those that change values due to a rare event or a failure, e.g., an air leak in a pressurized chamber. Impact parameters are defined as parameters that are either directly or indirectly controllable and may cause the rare event. These are the parameters that are of greatest interest for the determination of rare events.Step 2: Time SegmentationTime segmentation deals with partitioning and labeling the data into time windows (TWs). A time widow is defined as a set of observations in chronological order that describe a specified amount of continuous observations. This step allows the data mining algorithms to account for the temporal nature of the data. The most effective method to segment the data is bydetermining/estimating the approximate date of failure and set that as the last observation of the final time window.Step 3: Statistical and Visual AnalysisThis step involves statistical analysis of the data in each time period that was designated in the previous step. Process shifts, changes in variation, and mean shifts in parameters are helpful in indicating that the appropriate time windows and parameters were selected.Step 4: Knowledge ExtractionData mining algorithms discover relationships among parameters and an outcome in the form of IF … THEN rules and other constructs (e.g., decision tables) [1], [5]. Data mining is natural extension of more traditional tools such as neural networks, multivariable algorithms, or traditional statistics. In the detection of rare events, the decision-tree and rule-induction algorithms are explored for two significant reasons. First, the algorithms generate explicit knowledge in the form understandable by a user. The user is able to understand the extracted knowledge, assess its usefulness, and learn new and interesting concepts. Secondly, the data mining algorithms have been shown to produce highly accurate knowledge in many domains.Step 5: Analysis of Knowledge and ValidationThis step deals with validation of the knowledge generated by the data mining algorithm. If a validation data set is available it should be used to validate the accuracy of the rules. If no similar data is available then unused data from the analysis or a 10-fold cross-validation can be utilized [6].3 Power Boiler Case StudyThe approach proposed in this research was applied to power plant data. Data mining algorithms are well suited for electric power applications that produce hundreds of data points at any time instance.This case study deals with an ash fouling condition that causes boilershutdowns several times a year on a commercial 750 MW tangentially-fired coal boiler. The ash fouling causes a build up of material and pluggage in the reheater section of the boiler. Once the build up becomes substantial the boiler performance is negatively affected. This leads to the derating and the eventual shutdown of the boiler. The cleaning of the boiler during the shutdown requires 1 to 3 days. This problem is made more difficult by the fact there is no method to determine the level of ash build up without shutting down the boiler to physically inspect the area. Furthermore, in analysis all parameters were within specifications, so there was no obvious single parameter that is causing the pluggage. To investigate the problem considered in this paper, data was collected on 173 different boiler parameters. This included flows, pressures, temperatures, controls, demands, and so on. The data was collected in one-minute intervals over the course of three months. The data collection began directly following a shutdown where the reheater section of the boiler had no pluggage. The collection period ended approximately three months later when the boiler had to be shutdown for pluggage removal. This data set contained over 168,000 observations.The list of 173 parameters, which included both response and impact parameters, was analyzed. The list was reduced to include twenty-six impact parameters. This parameter categorization and reduction was accomplished with the assistance of domain experts as well as statistical analysis such as correlation and multivariate analysis.The initial step for time segmenting the data was to determine an approximate date for the failure event. In this application the failure event was defined by the date when the boiler was derated due to the pluggage. The cause of the shutdown was confirmed through visual inspection of the affected region. This date was then set to be the last day of the final time window (TW6).The windows were set to be approximately one week long. A week was chosen for several reasons. First, the boiler was inspected approximately onemonth prior to its derating. During the inspection the reheater section of the boiler was completely free of ash. This information provided the knowledge that the pluggage required less the one month to manifest itself to the point of shutdown. It was hypothesized that the pluggage requires several days to build up. Based on this information one week was deemed to be an adequate time window. One week also provided a sufficient number of observations (over 10,000 per window) for the data mining algorithms.Using the derate date and a one-week-long time window, the data was divided into six time windows shown in Figure 1. Time window 1 (TW1) was included to ensure that there was adequate data to describe normal operating conditions.There appears be a process shift between time windows 3 and 5 in Figures 1. The west tilt demonstrates a mean shift during window three and the hot reheat steam temperature displays a mean shift as well as a large increase in variation starting in time window four and culminating in window five. The results of this analysis lead to the hypothesis that the events that lead to the eventual pluggage occur between time windows three and five. It also confirms the selection of parameters and window size.The data mining approach was then applied to the data set to predict the predefined time windows (decision parameter). The algorithm produced a set of rules that described the parameter relationships in each time window.The knowledge extracted by the algorithm had an overall 10-fold classification accuracy of 99.7%. The confusion matrix (absolute classification accuracy matrix) is shown in Figure 2. The matrix displays the actual values and the values predicted by the rules during the cross-validation process.It can be seen from the data in Figure 2 that there are few predicted values that are off by more than one time window from the actual window. The results provided in the confusion matrix provide a high confidence in the proposed solution approach.Another test data set was extracted from the week following time window 1 and was labeled time window 2 (Test TW2). The last portion of the data (Test TW3) was obtained from the week after the generator was derated and the outcome was labeled time window 6 (TW6). The total test set contained over 30,000 observations.The rules and knowledge that were extracted from the original data set were then tested using the test data set. For purposes of analysis time windows1 – 3 were considered normal and time window 4 – 6 were considered faulty. The resulting confusion matrix is shown in Figure 3.The rules accurately predicted the normal cases, but they were not as effective in predicting the fault cases. This is most likely explained by the fact that the test data labeled, time window 6, was extracted after the boiler had been derated. The derating of the boiler significantly changes the combustion process and was not included in the original data set. In spite of this, the overall classification accuracy of the test data set is greater than 89%. The high cross-validation accuracy indicates that the rules accurately capture the changes in the process that lead to the ash fouling, pluggage, derating, and eventual shutdown of the boiler.4 Future ResearchEvent detection for control advisory systems has also been successfully demonstrated for applications that are dynamic and involve rare and catastrophic events [4]. Finch et al. [2] developed expert diagnostic information system, MIDAS, to alert users to abnormal transient conditions in chemical, refinery, and utility systems [3].The approach presented in this research produced rule sets that can be utilized for the development of a meta-control system. Integrating concepts from expert advisory systems and intelligent power control systems will form the meta-control system architecture for the avoidance of the ash pluggage.5 ConclusionIn this paper a data mining approach to predict failures was proposed and successfully implemented. The research utilized parameter categorization and time segmentation to overcome the limitation of traditional data mining approaches applied to temporal data. The proposed approach produced a knowledge base (rule set) that accurately described the subtle process shifts and parameter relationships that eventually may lead to the detection and avoidance of failures.This approach was applied to a commercial tangentially-fired coal-boiler to detect and avoid an ash fouling pluggage that eventually leads to boiler shutdown. The approach produced a rule set that was over 99.7% accurate. The knowledge base was also validated with a separate test data set that has predicted failures with accuracy of over 89.8%.The discovered knowledge will be used to develop an advance warning system reducing the number of boiler shutdowns. The intelligent warning system will have a significant economic impact. This translates into reduced cost to the consumer and a more efficient power industry.References1. Quinlan, J.R., “Induction of decision trees,” Machine Learning, vol. 1, no. 1, pp. 81-106, 1986.2. Branagan, L. A., and Wasserman, P. D., "Introductory use of probabilistic neural networks for spike detection from an on-line vibration diagnostic system", Intelligent Engineering Systems Through Artificial Neural Networks, vol. 2, pp. 719-724, 1992.3. Finch, F. E., Oyeleye, O. O., and Kramer, M. A., "Robust event-oriented methodology for diagnosis of dynamic process systems", Computers & Chemical Engineering, vol.14, no. 12, pp. 1379-1396, Dec, 1990.4. Pomeroy, B. D., Spang, H. A., and Dausch, M.E., "Event-based architecturefor diagnosis in control advisory systems", Artificial Intelligence in Engineering, vol. 5, no. 4, pp. 174-181, Oct, 1990.5. Pawlak, Z., Rough Sets: Theoretical Aspects of Reasoning About Data, Boston: Kluwer, 1991.6. Stone, M. "Cross-validatory choice and assessment of statistical predictions," Journal of the Royal Statistical Society, vol. 36, pp.111-147, 1974.附录B中文翻译燃煤锅炉的个案事故研究摘要这篇论文讲述了控制燃煤锅炉堵塞的方法。

毕业外文翻译焦炉设备的能源节约和环境改善资料

外文翻译Energy saving and some environment improvements in coke-oven plants焦炉设备的能源节约和环境改善学院： xxx学院专业：xxx学生姓名： xxx指导教师： xxx2014 年 04 月 16 日Energy saving and some environmentimprovements in coke-oven plantsAbstractThe enthalpy of inlet coal and fuel gas is discharged from a coke-oven plant in the following forms: chemical and thermal enthalpy of incandescent coke, chemical and thermal enthalpy of coke-oven gas, thermal enthalpy of combustion exhaust gas, and waste heat from the body of the coke oven. In recent years the recovery of several kinds of waste energy from coke ovens has been promoted mainly for energy saving purposes, but also for the improvement of environmental conditions. Among the various devices yet realized, the substitution of the conventional wet quenching method with a coke dry cooling is the most technically and economically convenient. The aim of this paper is mainly a review of the main types of coke dry cooling plants and a detailed examination of the infiuence of some parameters, particularly of temperature and pressure of the produced steam, and on the energy efficiency of these plants.1. Introduction1.1. Usable energyThe energy of a system-environment combination is usually defined as the amount of work attainable when the system is brought to a state of unrestricted equilibrium (thermal, mechanical and chemical) by means of reversible processes, involving only the environment at a uniformly constant temperature and pressure and comprising substances that are in thermodynamic equilibrium. Notwithstanding the quite different meaning, chemical energies differ from lower heating values slightly, as is discussed in [1,2]. The chemical energy generally falls between the higher and lower heating values but is closer to the higher.Nomenclaturec p constant pressure heat capacity [kJ/(kg K)]Ex energy [kJ]Ex u usable energy[kJ]ex specific energy[kJ/kg]G v volume flow rate [m3(nTp)/h]G v*specific volume flow rate [m3(nTp)/t dry coke]i specific enthalpy [kJ/kg]p pressure [bar]s specific entropy [kJ/(kg K]T temperature [︒C, K]T o environment temperature [︒C, K]v specific volume [m3/kg]Фenergy effciency [dimensionless]Nonetheless, the chemical energy is not suitable for quantifying the technical value of a fuel for two reasons: (i) Prior to considering heat transfer, it is necessary to account for the essentially irreversible combustion process, which decreases the exergies of various fuelsgreatly in different ways. (ii) The work corresponding to reversible expansion of several components (in particular CO2) down to their atmospheric partial pressures cannot be obtained from the combustion gas, as is implicit in the energyde®nition. In addition, this work differs with fuel type. Consequently, Bisio [3] defined usable energyas the exergetic value following an adiabatic combustion with a given excess air ratio (e.g., 1.1) minus the energyloss resulting from irreversible mixing of com-bustion gas with the atmosphere after having reached atmospheric pressure and temperature.The ratio of usable energyto lower heating value of a given fuel is termed the merit factor. This factor is always less than one and increases as the technical and economic values of a fuel rise.The parameter “usable exergy”, as has been de®ned and applied in [3], is suitable in the examin-ation of plants, that utilize fuel mixing, when the aim is to reduce both the total fuel consumption and, chiefly, the more valuable component one.1.2. Coke-oven energy recoveriesThe chemical energy of a fuel gas, which is used for a coke oven, amounts to 2500-3200 MJ/t dry coal. This energy, degraded to thermal energy of various operative values, is discharged from the plant in such forms:1.Thermal energy of incandescent coke (43-48%)2.Thermal enthalpy of coke-oven gas (24-30%)3.Thermal energy of waste gas (10-18%)4.Permeability, convection and radiation heat from the external surface of coke oven, and various losses (10-17%)The oil crisis of 1973 created a strong impulse towards a new thinking on the consumption and rational utilization of energy, particularly in the highly industrialized countries with limited indigenous energy resources. At the same time, attention throughout the world was also increas-ingly focused on environment problems.The possible utilization of the thermal energy of incandescent coke is dealt with in many papers . Usually, in coking technology the coke is cooled by being sprayed with water under special quenching towers. In recent years, the various types of dry cooling plants allow the recov-ery of nearly 80% of the thermal energy of incandescent coke. The possibilities of utilizing reco-vered energy are as follows:1.Production of steam and electricity.2.Preheating of coking coal.3.Room heating.The thermal energy of coke-oven gas, which is the second largest in the above listing, has so far been rarely utilized. Various studies, however, have been carried out for the possible utilization of this waste energy and a technique has recently been commercialized in Japan. The thermal energy of combustion exhaust gas is utilized to preheat both the combustion air and fuel gas mixture through a large-capacity regenerator. Consequently the waste gastemperature is reduced to approximately 200︒C. Lately, the further recovery of heat from waste gas has been reported in a few cases using a heat pipe installed in the ¯ue.The various kinds of heat wasted from the coke-oven external surface have been decreased by the reinforced sealing and better thermal insulation of coke ovens.In the following sections, the main types of coke-oven energy recoveries will be considered for a comparison.1.3. Protection of the environmentAs with the problem of energy saving and recovery, the last years have been characterized by increased prevention of atmospheric and water pollution by industrial emissions and domestic wastes. Work to control atmospheric pollution has been carried out in all developed countries. According to Zaichenko et al. , as a result of including measures for environmental protection, the investment and the coking costs are increased by 15%. However, if the calculations included allowance for losses caused by adverse effects of atmospheric pollution on workers health, instal-lation of engineering facilities for maintaining clean air can be cost-effective. In any case, it is obvious that an environmental facility is particularly tempting when, as with coke dry cooling plants, in addition to environment advantages, an energy recovery can be associated, even if the investment costs are higher and not justi®ed only by energy saving.2. Coke dry quenching2.1. Methods for energy recovery and saving from coke at the coke-oven outletThe idea of recovering thermal energy from incandescent coke by means of an inert gas dates back to the early 1900s. The ®rst industrial plants, designed particularly by the Sulzer Brothers (Winterthur, Switzerland) were carried out in the '20s and '30s both in the USA and in Europe (Germany, France, UK, Switzerland) [4,18]. However, the greater investment costs of dry quench-ing plants, in comparison with those of the wet quenching ones, were amortized with dif®culty in a period in which energy was very cheap. Consequently, dry quenching plants were given up.In the early 1960s, a new interest arose: in the USSR, dry cooling plants, which basically followed the Sulzer design, were built with the primary aim of preventing the coke from freezing in winter, as happens with wet quenched coke. The plant, constructed in various countries accord-ing to the Soviet Giprokoks process [6], is schematically shown in Fig. 1. The red-hot coke, at a temperature of about 1100︒C, is pushed from ovens, A, into containers placed on cars. Loaded cars are moved to the dry cooling plant, where containers, B, are lifted by bridgecrane, C, and unloaded through the charging system, D, into pre-chamber, E. Then,hot coke is transferred into the cooling chamber, F, in small batches. After leaving the cooling chamber through the discharg-ing system, G, coke runs, at a temperature of about 200︒C, ontoconveyor belt, H. Coke is refriger-ated by a circulating gas, composed mainly by nitrogen andmoved by the main blower, I. This gas transfers thermal energy in boiler, N, which produces superheated steam, O, at a pressure up to 100 bar. Before entering the boiler, the gas isscrubbed in the coarse de-duster, J, removing coarse particles of coke dust to protect the boilersurface from erosion. After leaving the boiler, the gas streams through the ®ne deduster, K, where ®ne dust is scrubbed out.In 1983 a dry cooling plant, schematically shown in Fig. 2, began operation in Germany. Its main characteristic is that 1/3 of the thermal energy is transferred directly from the coke to the vaporizing water and the remaining 2/3 through the inert gas. The advantages are a lower quantity of circulating gas with a correspondingly lower consumption of electrical energy by the blower and a greater energy recovery. Refrigerating walls in the cooling chamber represent the critical point of the plant i.In Germany, a combination of the coke dry cooling and coal preheating plant has been developed [5,9,14±16]. This system realizes primary energy saving (e.g. gas) instead of energy recovery of lower energyvalue (steam) and thus it is thermodynamically preferred (see, e.g., [29]). In addition, the well-known advantages of the single processes with respect to coke quality and increased output have been con®rmed. The completely closed system permits significant environmental improvements in the coking plant sector, avoiding the immissions of dust into the atmosphere in a practically complete way.Jung [13] considered the convenience of using water gas (H 2+CO) as the heat transfer fluid.Indeed, water gas has a thermal diffusivity three times that of nitrogen, and thus it allows us to reduce the boiler surface by 50%.In an anonymous note of “Metal Producing” [10], it was stated that the most convenient uses of the energy recovered from coke dry quenching (at least in the USA) are the following: the drying of coal and the heating of makeup water for boilers that provide steam in the coke plant per se. Indeed, the energy is available when the coke plant is running, which is of course when it is required. In addition, these quantities of energy match fairly well.2.2. Research on the optimal temperatures and pressures of steam2.2.1. Generalities about energy and energyanalysisIn Fig. 3 energy and energyflow diagrams are reported for a typical coke dry cooling plant with inlet coke temperature=1050°C and outlet coke temperature=200°C. Both diagrams are use-ful, however, only energyflow is suitable to visualize the operative value of the various energies.From Fig. 3 one remarks that with such devices it is possible to recover about 44% of the energyvalue of the incandescent coke thermal energy, corresponding to about the 20% of the energyvalue of the inlet coal.Owing to the relatively low value of the energyefficiency of a coke dry quenching system, it seems interesting to research the optimal values of some parameters, and in particular the charac-teristics of the steam produced (pressure and temperature) in order to obtain the more con-venient plant.A computer analysis has been made, assuming some input data, experimentally obtained from a recent actual plant. The input data are the temperature and pressure values of the gas flowing through the plant, the mass flow rates of coke at the inlet and outlet of the coke cooling chamber,and at the outlet of the coarse deduster, the mass flow rate, temperature and pressure of steam,the blower is entropic efficiency, and the efficiency in the electromechanical conversion of the electroblower. The fundamental data are:quenched coke mass flow rate 56 t/hsteam mass flow rate 28 t/hinlet coke temperature 1050°Coutlet coke temperature 200°Cspecific volume flow rate of gas 1650m 3 (nTp)/t dry coke.By varying the temperature and pressure of steam and/or the gas flow rate, one has determinedthe variation of the system energy efficiency, Ф , so defined:where: Ex st =steam exergy; Ex wa =boiler feed water; Ex c =energycorresponding to the electrical work of the electroblower; Ex co =coke physical energy(thus, excluding the chemical component of energy to be utilized in blast furnace).2.2.2. Specific energydependence upon temperature and pressureLet us consider specific energyas a function of temperature, T and pressure, p. In the diagram of Fig. 4, the steam specific energyfor an open system is reported as a function of pressure for various values of temperature. It is to be remarked that specific energyincreases always as T increases at constant p (for temperatures above that of the environment), whereas not always exincreases as p rises at constant T. This result seems puzzling and contrary to the concept of exergy.To justify the topic in a valid way, let consider the definition of specific energyfor an open sys-tem:and thenThe variation of specific enthalpy, di, and of specific entropy, ds, as a function of T and p can be written as [30]:and thenFrom these relations, one obtains that energyincreases as temperature rises, when T>T o , and the opposite is verified, when T<T o , as is well known. About the influence of pressure, one can say that energyincreases as pressure rises, when (T-T o .) and ∂1vtp have opposite sign, and, since with very few exceptions ∂1vtp> 0, when (T-T o )>0.When (T-T o ) and ∂1vtp have the same sign, one cannot exclude the possibility that exergy decreases when pressure goes up. This indeed is verified in a range in which the attractive forces are greatly prevailing on the repulsive forces [31]. For the problem that is here considered, this happens for superheated steam not far from the critical point. This analysis justifies that some is othermal curves of Fig. 4 have a maximum for a given pressure.On the other hand, this result could be yet puzzling. Indeed, it is well known that the operative value increases always with pressure. To this purpose, let us compare the following parameters:From these relations, in the range in which for the steam ∂2ex Tp <0 it follows:and then it follows that, if energydecreases as pressure goes down, the decrease of enthalpy is higher and consequently, even if the operative of the unit mass of steam goes down, the ratio of this operative value to the “cost” for obtaining it (i.e. the necessary heat) goes up and this is in agreement with the fact that a higher pressure is technically always more valuable. 2.2.3. Analysis results“Recovered exergy”has been determined; the numerator of relation (1) gives this parameter.As an example, in Figs. 5 and 6 the recovered energyis shown for one value of the specific volume flow rate of gas, alternatively, with steam pressure in abscissae (and temperature as parameter) or with steam temperature in abscissae (and pressure as parameter). One remarks that the recovered energygoes up almost linearly as the steam temperature increases, and goes up always as the steam pressure rises (contrary to the steam specific entropy), but with negative second derivative.In Fig. 7 the recovered energyis shown for one value of steam temperature as a function of the specific volume flow rate of gas (in abscissae) for various steam pressures (reported as parameter). To justify the diagrams, it must be remarked that as the specific volume flow rate of gas increases, the heat exchanged in the boiler between the gas and the water-steam increases with negative second derivative. Consequently, for every fixed couple of values of T and p, the team flow rate and the total steam energyexhibit the same behavior. On the contrary,owing to the increase of the necessary gas compression work, the recovered energyhas a maximum in correspondence with a given specific volume flow rate of gas. This maximum, for every temperature value, tends to a higher specific volume flow rate, as the pressure increases. In particular, at p=80 bar, the maximum is near to the value G v * =1650m 3 (nTp)/t dry coke .The variations of the energyefficiency, owing to its definition and the constancy of the physical energyof the incandescent coke, are totally similar to those of the recovered exergy. Thus, onlytwo diagrams for energyefficiency in correspondence to a specific volume flow rate of gasG v* =1650m 3 (nTp)/t dry coke are reported. In Figs. 8 and 9, energyefficiency vs steam pressure (with steam temperature as parameter) or vs the steam temperature (with steam pressure as parameter),respectively, is reported.On the basis of the various diagrams (not all here reported), the specific volume flow rate of gas G v* =1650m 3 (nTp)/t dry coke seems to be the more convenient. The very low increase of the recovered energy(and thus of the energyefficiency), that can be noted for some values of the couple (T, p) of the steam in correspondence to values of the specific volume flow rate of gas G v* slightly higher than 1650 m 3 (nTp)/t dry coke does not probably compensate the higher plant and maintenance costs.The temperature rise allows a remarkable energyefficiency increase. Thus, it seems convenientto choose the maximum temperature consistent with the use of materials which are not particularly expensive. The limit value of T=540°C can be presently chosen.As the pressure rises, energyefficiency increases remarkably till a pressure of about 80 bar, and then the increase is progressively reduced. For what is known to authors, the maximum value till now applied is of 103 bar in a steel plant of Japan. Thus, it seems that the more convenient pressure value is about 100 bar.焦炉设备的能源节约和环境改善摘要在下面几种形式中焦炉设备的进口煤和燃气的热量是不可控制的：炽热焦的化学和热焓，焦炉煤气的化学和热焓，燃烧排放气的热焓，还有从焦煤炉体中浪费的大量热量。

中英文翻译--电锅炉系统

中文2570字Electric Boiler SystemThe boiler to electric power for energy, heating through the electric heating tube heating, air conditioning or sanitation with hot water, heating it faster, high thermal efficiency, small size, no noise, modular heating, energy conservation, the installation of easy to use, a combination of all aspects of domestic and foreign advanced technology from the latest generation of products.Control PrincipleBoiler YLZK series used computer controller. I absorb advanced foreign technology companies, combined with domestic boiler control automation applications and specific needs of the status quo, the use of modern computer-controlled technology, and the introduction of a new generation of boiler controller. Apply to steam boilers, hot water boilers and automatic control of heat-conducting oil furnace, high reliability, high degree of automation, easy to use, easy to operate, feature-rich, flexible control, beautiful model, high cost performance.This machine adopts intelligent modular IPC (iPC) as the core control system. Smart Modular Industrial Computer (iPC) is a serial bus based on a variety of industrial control modules computer systems. As a result of the serial bus, which used more than ever parallel bus (such as STD, PC104, ISA, etc.) have more advantages. It is each module with a microprocessor (CPU) of the intelligent unit, itself a powerful programmable function independently of the unit features a variety of complex, computer controller boiler is the most advanced products.With the boiler water temperature control, boiler water level control, backwater temperature detection, the second backwater valve electric control, water protection, over-temperature protection, automatic control functions such as timing control.Control the plant-type electric boiler is a combination of various aspects of technology at home and abroad to form a new generation of products. It uses the principle of fuzzy control, combined with PLC controllers, temperature sensors, the system constitutes a closed-loop regulation. By temperature and the optimal operation of the principle of energy conservation, with changes in temperature, the temperature control system for continuous sampling, logic and artificial neural computing control algorithms adjust operations in order to achieve the purpose of automatic thermostat.Features(1) for the use of touch-screen interface, the realization of human-computerdialogue, easy-to-understand, easy to learn, easy to remember, easy to operate. Through the screen to check the function keys can be set and modify a variety of adjustment parameters.(2) the core system control PLC, great flexibility of its programmable logic processing capability with high speed and reliability.(3) organizations to adopt the international advanced the implementation of electrical components.(4) Controller with Built-in real-time clock calendar. System users can request, at any time to set up a number of different temperature settings to achieve the best energy-saving effect.(5) boiler control cabinet has a stop, over-temperature, over-pressure, short circuit, leakage, lack of phase, such as over-current protection, the boiler is running more stable and safe.(6) to peripheral storage boiler water storage tanks, the use of night-time trough of hot water heating to 95 ℃, storage tanks for storage, the day after the use of heat exchangers for heat exchangers for power grid Valley start-up the role of Tim Clipping run more economy.(7) boiler load function can be changed, health water and air-conditioning or hot water can be provided separately to provide cross-play of a machine or machines with multi-purpose use.(8) boilers to use the most clean energy - electricity, true green, zero emission, to maximize the protection of human life.Unit performance parameters Description:Rated hot water heating export / import Temperature: 85 ℃ / 65 ℃ (a backwater pressure electric water temperature: 95 ℃ / 70 ℃)Working pressure: atmospheric pressure (pressure electric water boiler and pressure 0.7MPa/1.0MPa)The scope for automatic adjustment of heat (no thermostat level) :10-100%Power: 380 ∨ 50HzAllowed outlet temperature: 85 ℃ (specification <90 ℃)All boiler water should be attached to GB1576-2001 "industrial boiler water" requirement.Boiler structureThe overall structure of the boiler and auxiliary equipment of two major parts.Boiler in the furnace, drum, burner, wall superheater, economizer, air preheater, furnace wall structure and composition of major components of the core of the production of steam, known as the boiler. Boiler in the two most important components are the furnace and the drum.Also known as furnace combustion chamber, fuel combustion for space. Will be on solid fuel on the grate for the fire-bed combustion furnace known as the layer burning stoves, also known as the fire-bed furnace; will be liquid, gas or ground into a powder of the solid fuel, is injected into the combustion chamber of the furnace of fire known as the Room burning furnace, furnace room, also known as the fire; air will hold its coal combustion was boiling and low-grade fuel for combustion furnace known as the boiling furnace, also known as the fluidized bed furnace; the use of coal particles of air flow so that high-speed rotation, and strongly burning furnace of cylindrical furnace known as the Tornado.Furnace cross-section of generally square or rectangular. Fuel combustion in the furnace flame and high temperature flue gas to form, so the stove around the furnace wall by the high temperature materials and thermal insulation materials. In the furnace wall on the inner surface of the regular laying of water-wall tube, it will not burn the protection of furnace wall and the flame and high temperature flue gas to absorb the large number of radiant heat.Furnace designed to take full account of the characteristics of the use of fuel. Each boiler shall be fueled with the original design as much as possible fuel. Burning characteristics of the larger difference in fuel economy when the boiler operation and reliability can be reduced.Drum is a natural cycle and multiple forced circulation boiler, the economizer to accept the water supply, circuit connection to the steam superheater cylinder delivery device described. Traditional drum made from high quality thick steel plate is a boiler in one of the most important components.Drum's main function is water, soft drinks to the separation of pot ruled out running in the saline water and mud residue, to avoid high concentrations of salt and impurities in the boiler water with the steam entering the superheater and the steam turbine in.Device includes an internal drum separator and steam cleaning equipment, water distribution pipes, sewage processing equipment such as drugs. Separator device which is to come from the wall and the saturated steam from the water and tominimize the steam in small water droplets carried. , The low-pressure boilers used as a baffle and baffle gap separating coarse components; over medium-pressure boiler in addition to a variety of widely used types of cyclone for the separation of rough, but also with 100 windows, steel mesh or steam, etc. are carried out further separated. Drum water level is also equipped with a table, a safety valve, such as monitoring and protection facilities.To assess performance and to improve the design, often have to go through the boiler heat balance test. Directly from the efficient use of energy to calculate the thermal efficiency of boiler is a balanced approach is called, from a variety of heat loss to the efficiency of counter-balance method is called counter-balance. Consider the practical benefits of the boiler room not only depends on the thermal efficiency of boilers, but also taking into account the auxiliary boiler and the amount of energy.Unit mass or unit volume of fuel combustion, the chemical reaction is calculated according to the theory of air known as air traffic demand. In order to make the fuel in the furnace, there are more opportunities for contact with oxygen combustion, the actual volume of air into the furnace is greater than the total theoretical air. Although more air into the incomplete combustion can reduce heat loss, but the smoke will increase heat loss, but also exacerbate corrosion of sulfur oxides and nitrogen oxides generated. Therefore efforts should be made to improve the combustion technology for small to minimize the excess air ratio so that the combustion chamber completely.Boiler flue gas contained dust (including fly ash and carbon black), oxides of sulfur and nitrogen pollution in the atmosphere are the material, without purification of their emission targets can be achieved several times indicators of environmental protection provisions of the several dozen times. Emissions control measures of these substances have a pre-combustion, improved combustion technology, dedusting, desulfurization and denitrification, such as. High chimney with only the area around the chimney to reduce atmospheric concentrations of pollutants.Flue gas dust removal of the force used by gravity, centrifugal force, inertia force of adhesion, as well as sound waves, static electricity and so on. Generally used for coarse particle sedimentation and inertial force of gravity separation, at a high capacity centrifugal separation under the regular use of electrostatic precipitators and bag dust filter with high collection efficiency. And the Sultan's wet - water film dust collector in the droplet adhesion film can fly, can absorb a very high collection efficiency of gaseous pollutants.The twentieth century since the 50's, people strive to develop comprehensive utilization of ash, Wei of harm. Ash manufacturers such as cement, brick and concrete aggregate and other construction materials. 70s extract from fly ash from Cenosphere, such as a fire-resistant insulation materials.Boiler future development will further enhance the thermal efficiency of boilers and power plants; boilers and power plants to reduce the unit cost of power equipment; to improve the operation of boiler unit level of flexibility and automation; to develop more varieties to suit different boiler fuel; raise the boiler unit and its the operation of auxiliary equipment reliability; to reduce environmental pollution.电锅炉系统该锅炉以电力为能源，通过电加热管加热供暖、空调或卫生用热水，该机加热快、热效率高、体积小、无噪音、模块式供热、节约能源、安装使用方便、综合了国内外各方面先进技术而成的最新一代产品。

毕业设计翻译---耐硫变换废热锅炉控制系统

基于模型预测控制利用不确定集方法的鲁棒优化摘要（原文上知网检索-The Robust Optimization Based Model Predictive Control using Box Uncertainty Set）论文考虑了鲁棒优化(RO)在模型预测控制中的应用。

这个优化方法包含了不确定数据，也就意味着当解决方案必须确定时优化问题的数据并不是精确的被知道。

鲁棒优化(RO)已经广泛应用于各种适用场合，在本文中，展现了在模型预测控制(MPC)中的应用。

基于模型预测控制的鲁棒优化(RO based-MPC)被用于废热锅炉控制的仿真模拟之中。

关键词：对偶问题，鲁棒优化，模型预测控制，内点法，二次模型性能I介绍MPC是一种控制算法，显性的使用过程的模型通过最小化一个目标函数。

这个模型被用来预测将来的过程输出。

众所周知，MPC在过程工业中处理限制性的多变量的控制问题。

知道过程输出，一个控制序列能够被计算用来简化设计的目标函数。

然而，工厂中每一步只用控制信号的第一个元素，这就是被熟知的区间后退策略。

在下一次采样时会重复上一次的计算方法。

在优化过程中，MPC用一个线性动态过程的模型，线性输入的限制，输出，和输入的减小量最终在一个最优控制的一次规划或二次规划中。

在这种情况中，工厂的动态的过程是不确定的，鲁棒MPC 已经有了解决了这个问题策略，适用于描述不确定性的一般方法工厂使用各种可用的数学模型文献中可用的框架。

接下来，考虑到闭环鲁棒性的一组性能指数会被选择。

鲁棒MPC然后通过在每个采样间隔求解鲁棒最优控制序列获得。

区间后退策略在每个采样间隔都被用来完成MPC算法。

这个方法降低了容量和大量的计算，用于能够处理不确定问题的优化项目。

最近，一种叫做RO的方法在数学编程和应用研究中被广泛研究。

RO方法被设计用来解决优化问题，当数据不确定或只知道不确定集中的数据。

这种方法最先被Ben-Tal和Nemirovski采用。

燃煤循环流化床锅炉外文翻译

英文文献翻译1；文献原文(1)Coal-Fired, Circulating Fluidized-Bed Boilers in ActionElectric utilities burning coal continueto search for cost-effective ways toincrease electricity generation whilestill meeting increasingly stringent emissionstandards. Over the last several years,fluidized-bed combustion has emerged as aviable option. One company with significant experience in the area of industrial andutility boiler design has developed a compact atmospheric internal recirculation circulating fluidized-bed (IR-CFB) boiler forcommercial application.Performance data for Babcock & WilcoxIR-CFB installations at Southern IllinoisUniversity (SIU) and an industrial facility inIndia are reported in a recent paper preparedby S. Kavidass and Mikhail Maryamchik ofBabcock & Wilcox (Barberton, Ohio),C. Price of SIU (Carbondale, Illinois), andA. Mandal of Kanoria Chemicals & Industries Ltd. (Renukoot, India). The paper, entitled ―B&W’s IR-CFB Coal-Fired BoilerOpe rating Experiences,‖ was presented atthe Fifteenth Annual International Pittsburgh Coal Conference, held September 14–18, 1998 inPittsburgh, Pennsylvania.IR-CFB Boiler DesignIn a fluidized-bed boiler, crushed coal isintroduced into a furnace containing a bedof either an inert material (like sand orcrushed limestone) or dolomite. Pressurizedair, fed into the bottom of the furnace, blowsupward through the bed and causes the coaland bed materials to ―fluidize‖ in a highlyturbulent, suspended state. Figure 1 profilesa typical IR-CFB furnace, demonstrating thechange in bed density with increasingheight. The turbulence of the fluidized-bedsystem allows prolonged contact betweenthe air and the particles of coal, resulting inmore complete combustion at a lower temperature than older systems (which reducesnitrogen oxides). If sorbent material such aslimestone is used as bed material, emissionsof sulfur dioxide are likewise reduced due toconversion to calcium sulfate. Further, because combustion occurs at a lower temperature, the process is relatively insensitiveto the type of fuel burned. This allows theuse of alternative fuels such as coal waste,biomass fuels, petroleum coke, and otherlower British thermal unit (Btu) material.A circulating fluidized bed captures thesolids carried out of the furnace and returnsthem to the primary combustion chamber.This recycling feature increases the fuel residence time in the furnace, which increasescombustion efficiency. The Babcock &Wilcox IR-CFB boiler provides two stagesof solids recirculation, maximizing fuelburnout and sulfur capture. Also, designvelocities at the furnace exit are relativelylow, which significantly reduces erosion ofthe upper furnace and primary solids separator.Unique Design FeaturesOne of the features of Babcock & Wilcox’s IR-CFB design is the use of a U-beamsolids separation system. As shown in Figure 2, the U-beam system consists of rowsof U-shaped vertical rods attached to theroof of the furnace that interrupt the flow ofthe gases exiting the furnace. Two rows ofU-beams are placed inside the furnace itself,and four rows of U-beams are installed behind the furnace rear wallplane. The in-furnace U-beams capture about 75% of thesolids, which slide down the length of thebeams back into the combustion chamber.The remaining solid particles captured in theexternal U-beams are collected in a particlestorage hopper, which is periodically emptied back into the furnace forreburning.Theflue gas velocity across the U-beams isaround 8 meters/second (26.5 ft/sec) or less,producing a relatively low gas-side pressuredrop (less than 1 inch of water column) ascompared to conventional cyclone-typeseparators (6 to 10 inches of water column).The IR-CFB furnace is made of gas-tightmembrane enclosure water-cooled wallswith studded tubing spaced every fourinches. The lower furnace walls (up to aheight of 7.3 meters [24 ft]) are protectedwith an ultra high-strength, abrasion-resistant, low-cement refractory material lessthan 1 inch in thickness, which is placedover the studs protruding from the coolingtubes. A band of metal spray is typicallyapplied to further protect against erosion atthe point where the refractory material ends.The very thin application of refractory material means faster startup and less maintenance cost.Other beneficial characteristics of the IR-CFB boiler design include:* Use of in-furnace surfaces (division andwing walls) for furnace temperature control;* Gravity fuel feed and simplified secondary ash recycle system;* Absence of hot expansion joints, allowingsignificantly reduced maintenance;* Smaller footprint, which allows retrofitinside existing structural steel.Operating Experience at Two InstallationsThe IR-CFB design has been installed attwo locations—one at SIU in Carbondale, Illinois, and the second at the KanoriaChemicals & Industries Ltd. (Kanoria) sitein Renukoot, India. The SIU installation is a35-megawatt (MW) boiler that burns high-sulfur, low-ash Illinois coal, while the 81-MW Kanoria unit uses low-sulfur, high-ashcoal. The SIU boiler has a crushed limestonebed to combat the higher sulfur content ofthe fuel, while the Kanoria boiler uses a sandbed.SIU Unit dataThe SIU boiler is located close to the OldBen II coal mine in southern Illinois. Theplant was completed in 1996 and startedoperation in mid-1997. Performance testingwas completed in September 1997. Table 1shows the design and performance data forthe SIU boiler.Raw coal, delivered by truck, is movedby drag chain conveyor to a crusher. A24-hour capacity silo stores the pulverizedcoal. The coal is introduced into the furnaceby one gravimetric feeder through the sidewall. Two 60-MMBtu/hr gas-fired, over-bed burners and two 25-MMBtu/hr gas-fired, in-bed lances provide heat for startup.A multi-cyclone dust collector is used as asecondary solids separator (downstreamfrom the U-beams). The overall solids collection efficiency exceeds 90% and solidscollected in the cyclone are returned to thefurnace via an air fluidized conveyor. Abaghouse provides final particulate control.The bed material is periodically drainedfrom the furnace to control bed solids build-up and to remove any oversized material.The SIU unit has a single 8-inchdiameterdrain pipe to remove the bed, which iscooled with a screw ash cooler using recirculated plant water supply.Cold startup to 100% maximum continuous rating (MCR) can be achieved withinfive hours and the observed boiler dynamicload response is 5%–6% per minute. Aboiler turndown of 5:1 has been achievedwithout auxiliary fuel (a turndown ratio of3.5:1 to 4:1 is guaranteed). Further, all majorequipment has performed reliably whilemeeting or surpassing permitted emissions.A soot blower installed at the horizontalconvection pass floor has experienced plugging with ash and residual moisture. Whilethe boiler can operate successfully withoutthe soot blower, more investigation isneeded to overcome this operational glitch.Kanoria Unit DataThe Kanoria facility is located within thestate of Utter Pradesh, India, in close proximity to the Singaroli coal mine. The boilerwas constructed in 1996 and began commercial operation in February 1997. Performance testing continued until September1997. Design and performance data for theKanoria boiler are also shown in Table 1.In contrast to the Illinois coal, the Kanoriafuel is erosive, low in sulfur, and high in ash.Crushed coal is introduced via two volumetric drag chain feeders through the front wallof the furnace. Two 60-MMBtu/hr oil-firedover-bed burners provide heat for startup.Solids collected by the U-beams are reinjected by gravity into the furnace at fourlocations. The Kanoria unit uses an electro-static precipitator for final particulate control. Bed draining is accomplished throughtwo bed drain pipes and ash coolers; finematerial is returned to the furnace, whileoversize particles are diverted to the ashdisposal system.The observed boiler efficiency of 88.8%is higher than originally anticipated andcombustion efficiency has exceeded 99%,due to very low unburned carbon and lowflue gas outlet temperatures. However, theerosive nature of the fuel initially causedtubing leaks in the water-cooled furnacewall, which have been remedied by applyingadditional metal spray at the refractory interface and adjusting the interface angle.Also, furnace temperature exceeded designvalue on several occasions due to insufficient upper furnace inventory caused by failures of the first fields of the electrostaticprecipitator and the ash conveying system.Adjustments to the precipitator rectifier andthe ash silo backpressure have solved theseproblems.In summary, two examples of IR-CFBboilers are successfully operating at 100%MCR with varying fuel types. IR-CFB appears reliable and incorporates several verylow-maintenance features that reduce operating costs.（2）Why Build a Circulating Fluidized Bed Boilerto Generate Steam and Electric PowerAbstractIn Asia, demand for electric power continues to rise steeplydue to population growth, economic development, and progres-sive substitution of alternate technologywith clean forms ofenergy generation. Atmospheric circulating fluidized bed (CFB)echnology has emerged as an environmentally acceptable technology for burning a wide range of solid fuels to generate steamand electricity power. CFB, although less than 20 years old, is amature technology with more than 400 CFB boilers in operation worldwide, ranging from 5 MW e to 250 MW e.Electric utilities and Independent Power Producers must nowselect a technology that will utilize a wide range of low-costsolid fuels, reduce emissions, reduce life cycle costs, and provide reliable steam generation for electric power generation.Therefore, CFB is often the preferred technology. Even thoughpulverized coal (PC) fired boilers continue to play a major roleworldwide, they have inherent issues such as fuel inflexibility,environmental concerns and higher maintenance costs.This paper discusses the benefits of CFB boilers for utilityand industrial applications. Specific emphasis is given to B&W’snternal Recirculation CFB (IR-CFB) technology, CFB technology comparisons, PC vs. CFB technology, emissions benefits,and economics including maintenance cost and boiler reliabilty. IntroductionBabcock & Wilcox (B&W) is a leading global supplier ofindustrial/utility boilers and has supplied more than 700 unitstotaling more than 270,000 MW e. Many of B&W’s CFB boilerdesign features have been adapted from vast experience designing and building boilers of all types and sizes for industrial andelectric utility applications. B&W’s design is an inherently compact, distinctive internal recirculation fluidized bed (IR-CFB)boiler featuring U-Beam solids separators. The furnace and convection pass of the IR-CFB boiler are within a single, gas–tightmembrane enclosure as commonly found in Pulverized Coal(PC) fired boilers. This CFB technology has been successfullyintroduced in the global market.To date, B&W, including B&W joint ventures and licenseecompanies, has sold 16 CFB boilers worldwide, shown in Table 1.B&W offers IR-CFB boilers up to 175 MWe, both reheat andnon-reheat, with full commercial guarantees and warranties. TheIR-CFB boiler is simple in configuration and compact, requiresa smaller boiler foot print, has minimal refractory, requires lowmaintenance, features quick startup, and provides high avail-ability.The modern way of burning solid fuels requires fuel flex-ibility and reliable technology, plus good combustion efficiencywith low emissions. CFB technology is well suited for a widerange of sold fuels. CFB technology is proven, mature and competitive.What is CFB technology?CFB technology utilizes the fluidized bed principle in whichcrushed (6 –12 mm x 0 size) fuel and limestone are injectedinto the furnace or combustor. The particles are suspended in astream of upwardly flowing air (60-70% of the total air) whichenters the bottom of the furnace through air distribution nozzles.The balance of combustion air is admitted above the bottom ofthe furnace as secondary air. While combustion takes place at840-900 C, the fine particles (<450 microns) are elutriated outof the furnace with flue gas velocity of 4-6 m/s. The particlesare then collected by the solidsseparators and circulated back into the furnace. This combustion process is called circulatingfluidized bed (CFB). The particles’ circulation provides efficient heat transfer to the furnace walls and longer residence timefor carbon and limestone utilization. Similar to PC firing, thecontrolling parameters in the CFB combustion process are temperature, residence time and turbulence.Designers and power plant operators have vast experience in PC-fired boiler design and operations. Adapting and under-standing CFB technology by those familiar with the PC environment requires time. CFB technology brings the capability ofdesigns for a wide range of fuels from low quality to high quality fuels, lower emissions, elimination of high maintenance pulverizers, low auxiliary fuel support and reduced life cycle costs.A PC vs. IR-CFB comparison is given in Table 2.The combustion temperature of a CFB (840-900 C) is muchlower than PC (1350-1500 C) which results in lower Nox for-mation and the ability to capture SO2with limestone injectionin the furnace. Even though the combustion temperature of CFBis low, the fuel residence time is higher than PC, which resultsin good combustion efficiencies comparable to PC. The PC pulverizers, which grind the coal to 70% less than 75 microns, require significant maintenance expenses. These costs are virtually eliminated in CFB because the coal is crushed to 12 - 6 mmx 0 size. Even though CFB boiler equipment is designed forrelatively lower flue gas velocities, the heat transfer coefficientof the CFB furnace is nearly double that of PC which makes thefurnace compact. In an IR-CFB, auxiliary fuel support is neededfor cold startup and operation below 25% versus 40-60% MCRwith PC. One of the most important aspects is that CFB boilers release very low levels of SO2 and NO x pollutants compared to PC, as shown in Table 2. PC units need a scrubber system, whichrequires additional maintenance.CFB is a fuel-driven and flexible technologyCFB can be the technology of choice for several reasons.The CFB can handle a wide range of fuels such as coal, wastecoal, anthracite, lignite, petroleum coke and agricultural waste,with low heating value (>1500 kcal/kg), high moisture content(< 55%), and high ash content (< 60%). The fuel flexibility provides use of opportunity fuels where uncertainty of fuel supplyexists and economics are an issue. If a CFB boiler is designedfor coal, the same boiler can be used to burn lignite or petroleum coke or anthracite. The material handling and feeding system should be properly designed to meet these fuel variations.Such fuel flexibility is not available in the competing conventional PC-fired boiler technologies. This is one of the importantfeatures of CFB that the customer needs to analyze carefullybefore selecting a technology.Environmental benefits of CFB technologyThe CFB combustion process facilitates steam generationfiring a wide range of fuels while meeting the required emissions such as sulfur dioxide (SO2 ) and nitrogen oxides (NO x)even more effectively than World Bank guidelines, as shown inTable 3.The major environmental benefit of selecting CFB technology is the removal of SO2(90-95%) and NO x(emission is lessthan 100 ppm) in the combustion process without adding postcombustion cleaning equipment such as wet or dry flue gasdesulfurization (FGD) systems and selective catalytic reduction(SCR) systems. When the limestone is injected into the furnace,the following reactions occur.* Oxidation of sulfurS+O2 --> SO2* Limestone is calcined to form calcium oxideCaCO3--> CaO + CO2–425 kcal/kg (of CaCO3 )* Sulfur dioxide gas reacts with solid CaOSO2+ 1/2 O2 + CaO --> CaSO4 (Solid) +3740 kcal/kg (of S) The resulting calcium-sulfate-based ashes are chemicallystable and are easily disposed. This ash can be used as raw material for cement manufacturing, soil stabilization, concreteblocks, road base, structural fills, etc. Limestone injection isrequired for fuels with sulfur greater than >0.5%. Lime (CaO)and unburned carbon content must be considered in re-use applications, depending on the fuel being fired.NO x present in flue gas generally comes from two sources:the oxidation of nitrogen compounds in the fuel (fuel NO x) andreaction between the nitrogen and oxygen in the combustionair (thermal NO x). With low temperature and staged combustion,the oxidation of fuel nitrogen is suppressed resulting in verylow NO x emissions. NO x emissions are <100 ppm with CFB.CO and hydrocarbon emissions in the CFB boiler are wellcontrolled. In recent years, financial institutions have pushedthe power project developers to meet the World Bank emissionsrequirements. Therefore obtaining the project permit is less difficult with CFB technology.Design features of B&W IR-CFB Boiler technologyB&W IR-CFB technology is very comparable to PC-firedboilers in arrangement. The IR-CFB boiler design consists ofthe following major systems, shown in Fig. 1. The main CFBboiler components are:* Boiler furnace* Furnace bottom air distributor and nozzles* Primary solids separators and recirculation system* Secondary solids separators and recirculation system* Pendant superheater / reheater* Economizer and horizontal tubular air heater* Air assisted gravity fuel /limestone feed systemBoiler FurnaceThe furnace cross section is selected based on flue gas superficial velocity. B&W typically uses furnace depths of 3.7 m,4.6 m and 5.4 m, depending on the unit size. The furnace enclosure is made of gas-tight membrane water-cooled walls having63.5 mm or 76 mm tube diameters on 102 mm centers. The furnace primary zone is reduced in plan area cross section to provide good mixing and promote solids entrainment at low load.The auxiliary startup burners, fuel feed points and secondaryash re-injection (multicyclone/MDC) points are located in thisregion.A thin layer of refractory is applied on all lower furnace walls,including the lower portion of the division walls and wing wallnose to protect against corrosion and erosion. An ultra highstrength abrasion-resistant low cement alumina refractory 16-25 mm thick is applied over a dense pin studded pattern. B&Whas patented aRDZ TM reduced diameter zone feature that elimihas nates erosion concern at the furnace interface. The furnace temperature is precisely controlled by maintaining proper inventory and thus the combustion efficiency and the limestone utili-zation are maximized.Air Distrbutors and NozzlesThe furnace bottom air plenum or wind box is made of water-cooled panels or casing depending on startup air temperature. Bubble caps are fitted on the water-cooled distributor floorpanels as shown in Fig. 2. The bubble caps are designed to distribute air uniformly, prevent the back sifting of solids at lowload operation, and create good turbulence for fuel /sorbentmixing in the primary zone. The bubble caps are spaced 102mm x 117 mm with 60-70% of total combustion air admittedthrough the bottom. The balance 30-40% of total air is admittedthrough overfire nozzles (high velocity) in the front and rearfurnace walls.Primary Solids SeparatorsThe solids separation system is a key element of any CFBboiler design. The B&W separation system is designed for thelife of the unit without replacement, influencing life cycle costs.The B&W IR-CFB has a two stage primary solids separator asshown in Fig. 3, comprised of in-furnace U-Beam separatorsand external U-Beam separators. The in-furnace U-Beams (tworows) are able to collect nearly 75% of the solids. The remaining solids are collected by the four rows of external U-Beamsand are discharged from the hopper directly into the furnace throughthe transfer hopper located beneath the external U-Beams (See Fig.4). The flue gas velocity across the U-Beams is approximately 8-10 m/s, limiting the gas-side pressure drop to 0.25 kPa as compared with a typical cyclone separator’s pressure drop of 1.5 to 2.0kPa. A commercially available, high-grade stainless steel materialis used for the U-Beam separators.Secondary Solids SeparatorThe multicyclone dust collector (MDC) is located in the convective pass either upstream or downstream of the economizer.The MDC typically has a top inlet and top outlet as shown inFig. 5. The MDC tube diameter is normally 229 mm arrangedover the second pass entire cross section. The MDC providesoutstanding retainment of fine particles up to 50 microns. TheMDC collection tubes and spin vanes have high hardness (550BHN), designed for longer life and easy replacement duringplanned outages.The small quantities of fines which escape from the externalU-Beams are collected by the MDC. The collected fines arestored in the MDC hopper. Variable speed rotary feeders or inclinedscrews are used to control the ash recycle flow rate fromthe hopper. Precise furnace temperature control is achieved byadjusting the speed of the rotary feeders or inclined screws, taking the temperature signal from the furnace.The superheater may consist of vertical pendant type primary and secondary banks, located in the convection pass, aswell as surface in the furnace in the form of superheater wingwalls. An attemperator is used to control the final steam temperature over the design load range. The flue gas velocities arerelatively low and selected byconsidering the dust loading andash erosivity of the fuel. When required, the reheater is locatedin the convection pass, and steam bypass is recommended tocontrol the final reheater temperature.Economizer and Horizontal Tubular air heaterThe economizer is designed with tubes running front to backin an in-line arrangement. Flue gas velocities used consider thedust loading and ash erosivity of the fuel. If the MDC is locatedupstream of the economizer, higher velocities are used and boththe economizer and the air heater are located in an in-line arrangement to minimize ash fouling. The air heater is locatedafter the MDC and the economizer. The flue gas is outside thetubes and air is passed through the tubes. A hopper is providedat the bottom of the air heater and the ash collected in the hopper is purged to the ash disposal system. The tube material andflue gas velocities are selected by considering the dust loadingand the ash erosivity of the fuel. A steam coil air heater (SCAH)is used to protect the cold end of the air heater if required.Air-Assisted Gravity Fuel/Limestone Feed SystemFuel handling and feeding is one of the major challenges inCFB boiler operation, especially with waste fuels because ofhigh fines and moisture content. The crushed fuel (6-12 mm x0) is stored in the silo, usually located in front of the boiler asshown in Fig. 6. Fuel is fed to the boiler via down spout fromsilo discharge to feeder and a series of feeders and gravity feedchutes. The fuel chute will have at least a 65 degree angle fromhorizontal. Primary air is used to sweep the fuel into the furnace and as seal air to the feeders. The number of feed points isset to achieve even fuel distribution in the furnace.The limestone handling and feeding system is relativelysimple compared to the fuel feed system. Limestone is fed either pneumatically or mechanically into the CFB boiler. Thepneumatic system feeds the limestone directly into the furnacethrough furnace openings in the front and rear walls. In themechanical system, the limestone is fed into the discharge endof the fuel feeders via rotary feeders. The limestone falls bygravity down the fuel feed chute with the fuel into the furnace,and is a function of fuel velocity and required emissions.CFB Technology ComparisonVirtually all major boiler manufacturers are involved inCFB technology. Two distinct types of solids separation systems are used. One type is cyclone–based, which provides singlestage solids collection systems, and the second type is impactseparator-based, which provides a two-stage solids separationsystem. A comparison of B&W IR-CFB technology features withthose of other major commercial CFB technologies is given inTable 4.Advantages of the B&W IR-CFB Boiler technology*Boiler is compact with primary U-Beam separators andprovides internal solids recycle.* Boiler has a smaller foot print (up to 20 to 30% less building volume compared to a hot cyclone-based CFB boiler)* Boiler design is especially suitable for retrofitting of olderPC-fired boilers within the existing support steel.* Two-stage solids separation efficiency (>99.7%) provideshigher carbon efficiencies and better limestone utilization through higher solids residence time.* Wide turndown ratio (4:1) without auxiliary fuel is possible due to the selection of furnace velocity and control-lable solids recycle.* Less refractory in the boiler allows for quicker startupand lower maintenance costs.Economics of CFB TechnologyCFB technology can burn a wide range of low cost solidfuels and competes well with oil/gas fired plants. The decision-makers often ask, ―What are capital and operating costs andbenefits of a CFB boiler?‖ The experience in Europe and NorthAmerica suggests that for a sulfur fuel (>0.5%S) and less than150 MW, a CFB boiler has 8-15 percent lower capital costs aswell as 5-10% lower operating costs than a PC-fired boiler because of the FGD system. In general, CFB-based power plantsprovide low emissions control costs and low O&M costs, whichlead to lower life cycle costs. In the end, owner profit marginincreases and payback period improves as shown in Table 5.Costs not included in Table 5 are items such as land, projectdevelopment, permitting, escalation, taxes and owner’s costs,since these costs are common for both PC and CFB-based powerplants.Reliability of CFB TechnologyCFB boiler design is simple and proven, compared to othertechnologies. Experience indicates that operating and maintenance costs are relatively lower than PC-fired boilers becauseof the ability to burn lower rank fuels, thus reducing fuel costescalation uncertainty. Since maintenance areas are very minimal in the CFB boiler, the availability of the boiler is relativelyhigher. The CFB design allows emissions reduction without significant capital cost, since SO2 and NO x removal are inherentwithin the combustion process.ConculusionEven though a number of competing technologies areavailable in the market for steam and electric power generation, CFB is an excellent choice due to its fuel flexibility, widerturndown without support oil/gas, superior environmental performance, lower operating and maintenance costs, and safe, reliable and simple boiler operation. The B&W IR-CFB boilerdesign offers compact, superior performance due to two-stagesolids separation, and is cost effective for multiple fuel firingin both PC retrofit and greenfield applications.2；译文（1）燃煤循环流化床锅炉运行情况燃煤发电行业继续搜寻成本效益的方式,以增加发电量,同时达到日益严格的排放标准. 过去几年,流化床燃烧已成为一种可行的选择. 一个公司有重大领域的经验,工业及电站锅炉设计开发了紧凑型大气内部循环流化床(红外CFB )锅炉投入商业应用.Babcock & Wilcox的红外流化床装置, 最近在南伊利诺伊大学和印度的一个工业设施中，在一份由S.kavidass和米哈伊尔Maryamchik的Babcock &Wilcox (巴伯顿,俄亥俄州) , C.SIU(代尔,伊利诺州) ,和A的[27]卡诺里亚&化学工业有限公司( renukoot ,印度) 被报道 . 这份文件题为"巴威的红外循环流化床燃煤锅炉的操作经验" ,并提交于15年度国际匹兹堡煤炭会议于9月14-18 , 1998年在匹兹堡,宾夕法尼亚州.红外型循环流化床锅炉设计在循环流化床锅炉，煤粉被引入炉膛内的床上，其中包含或惰性物质（如砂或粉碎石灰石）或白云石。

电厂锅炉英文文献

电厂锅炉英文文献以下是一篇关于电厂锅炉的英文文献，供参考：Title: Boiler in Power Plant - A ReviewAbstract:Boilers play a crucial role in power plants, providing steam for electricity generation. This paper reviews the various types of boilers used in power plants, their working principle, and the challenges faced in their operation. It also discusses the importance of efficient boiler performance in ensuring reliable power generation.Introduction:Power plants heavily rely on boilers for steam generation, which in turn drives the turbines to generate electricity. Boiler technology has evolved significantly over the years, with advancements in efficiency, reliability, and environmental friendliness. This review provides a comprehensive overview of boiler technology in power plants, highlighting the key components and their functions. Types of Boilers:There are several types of boilers used in power plants, including pulverized coal-fired boilers, circulating fluidized bed boilers, and supercritical boilers. Each type has its unique characteristics and advantages. Pulverized coal-fired boilers are the most common type, where coal is ground into fine particles and burned in a furnace to produce steam. Circulating fluidized bed boilers use a bed of sand and fuel particles to achieve efficient combustion. Supercritical boilers operate at high pressures and temperatures toimprove efficiency.Working Principle:Boilers operate on the principle of heat transfer from the combustion of fuel to the working fluid, typically water or steam. Fuel is burned in the furnace, generating heat that is transferred to the water/steam in the boiler tubes. The heat transfer process is facilitated by convection and radiation. The resulting steam is then used to drive the turbines for electricity generation.Challenges in Boiler Operation:Boiler operation faces several challenges, including maintaining high efficiency, controlling emissions, and ensuring safety. Efficiency is crucial as it directly impacts the overall power plant performance. Design and operational factors affect boiler efficiency, and continuous monitoring and optimization are required to maximize efficiency. Emission control is also a significant challenge, as power plants are subject to strict environmental regulations. Lastly, safety considerations are paramount to prevent accidents and ensure the well-being of personnel.Conclusion:Boilers are vital components in power plants, responsible for steam generation and subsequently electricity production. Understanding the different types of boilers, their working principles, and the challenges in their operation is essential for efficient and reliable power generation. Ongoing research and development in boiler technology aim to further improve efficiency, reduce emissions, and enhance safety in power plant operations.。

锅炉专业英语中英文对照表

锅炉专业英语中英文对照表火道锅炉Flame tube boiler疏水器、疏水阀steam trap饱和蒸汽saturated steam过热蒸汽superheated steam震动炉篦Oscillating bar grate链条炉蓖Chain grate, travelling grate省煤器economizer减速器speed reducer螺旋除渣机screw slag remover除尘器dust collectorcombustion air fan鼓风机exhausting fan上煤机coal conveyor尖端的、高科技的Hi-tech节能的energy-saving高效的high-efficiency低噪声的low noise耐用的、持久的durable蒸发evaporation额定的rated热效率thermal efficiency碳化物carbide碳化硅silicon carbidemonoxide一氧化碳carbon monoxide二氧化碳dioxide二氧化碳亚临界压力锅炉carbon dioxide subcritical pressure boiler燃煤锅炉coal-fired boiler启动锅炉 start-up boiler炉墙 furnace wall管束（排） tube bundle管屏tube platen下降管 downcomer上升管 riser省煤器管 economizer tube再热器管 reheater tube过热器管 superheated tube蛇形管 coil吊挂管 supporting tube水冷壁管 water wall tubesaturated steam pipe水冷壁 water wall鳍片管finned tube, fin tube, gilled tube 联箱 header锅炉本体 boiler proper锅炉机组 boiler unit炉膛 boiler framework燃烧器 furnace燃烧室 combustion chamber油枪 oil gun torch风门 damper管板 tube plate。

锅炉专业中英文对比

boiler锅炉boiler unit锅炉机组stationary boiler固定式锅炉steam boiler/generator蒸汽锅炉utility boiler电站锅炉industrial boiler工业锅炉hot water boiler热水锅炉indoor boiler室内锅炉outdoor boiler露天锅炉package boiler快装锅炉shop-assembled boiler组装锅炉field-assembled boiler散装锅炉field-erected boiler 超临界压力锅炉supercritical pressure boilersubcritical pressure boiler亚临界压力锅炉superhigh pressure boiler超高压锅炉high pressure boiler高压锅炉medium pressure boiler中压锅炉low pressure boiler低压锅炉natural circulation boiler自然循环锅炉forced circulation boiler强制循环锅炉assisted circulation boiler辅助循环锅炉controlled circulation boiler控制循环锅炉once-through boiler直流锅炉combined circulation boiler复合循环锅炉low circulation-ratio boiler低循环倍率锅炉solid-fuel fired boiler固体燃料锅炉liquid-fuel fired boiler液体燃料锅炉coal fired boiler燃煤锅炉oil fired boiler燃油锅炉gas fired boiler燃气锅炉multi-fuel fired boiler混烧锅炉boiler with dry-ash furnace固态排渣锅炉boiler with dry-bottom furnaceboiler with slag-tap furnaceboiler with wet-bottom furnacesupercharged boiler增压锅炉water tube boiler水管锅炉cross drum boiler横锅筒（汽包）锅炉longitudinal drum boiler纵锅筒（汽包）锅炉shell boiler锅壳锅炉horizontal boiler卧式锅壳锅炉vertical boiler立式锅炉stationary boiler of locomotive type固定式机车锅炉π-type boiler（two-pass boiler)π型锅炉box-type boiler箱型锅炉tower boiler塔型锅炉D-type boilerD型锅炉rated capacity额定蒸发量nominal capacity最大连续蒸发量maximum continuous ratingrated heating capacity额定供热量nominal steam condition额定蒸汽参数nominal steam parameter额定蒸汽压力nominal steam pressurenominal steam temperature额定蒸汽温度(nominal) hot water temperature热水温度feed water temperature给水温度return water temperature回水温度circulation circuit循环回路steam generating circuit蒸汽净化steam purificationsteam temperature control汽温调节feed water给水condensate凝结水make-up water补给水boiler water锅水；炉水boiling crisis沸腾换热恶化as-fired fuel炉前燃料fire bed火床fuel bed最高火界fire lineadditive添加剂flue gas dew point烟气露点boiler circulation水循环mechanical carry-over机械携带moisture carry-over溶解携带vaporous carry-overwater separation汽水分离steam washing蒸汽清洗stage evaporation分段蒸发pressurized firing压力燃烧negative-pressure firing负压燃烧grate firing火床燃烧suspension firing火室燃烧；悬浮燃烧tangential firing切向燃烧opposed firing对冲燃烧cyclone-furnace firing旋风燃烧fluidized-bed combustion沸腾燃烧gas recirculation烟气再循环natural draft自然通风mechanical draft机械通风balanced draft平衡通风forced draft正压通风induced draft负压通风zone control分段送风pressure atomization压力雾化；机械雾化mechanical atomization双流体雾化twin-fluid atomizationrotary-cup atomization旋杯雾化；转杯雾化direct leakage直接泄漏infiltration leakage间接泄漏bypass leakageentrained leakage锅炉本体boiler properheating surface受热面radiant heating surface辐射受热面convection heating surface对流受热面pressure part受压部件；受压元件cylindrical shell筒体head封头；端盖header集箱；联箱tube panel管屏up flow riser tube panel垂直上升管屏ribbon panel回带管屏spirally-wound tubes水平围绕管圈tube bundle管束gas pass烟道gas duct对流烟道convection passparallel gas passes并联烟道air duct风道arch拱furnace arch折焰角water-cooled hopper bottom冷灰斗wall with refractory lining卫燃带refractory belt悬吊管supporting tubedesign pressure设计压力maximum allowable working pressure最高允许工作压力maximum allowable metal temperature最高许用壁温furnace enclosure design pressure炉膛设计压力heat input输入热量heat output锅炉有效利用热量fuel consumption燃料消耗量calculated fuel consumption计算燃料消耗量ash-retention efficiency排渣率load range at constant temperature（保持）额定汽温的负荷范围injection flow(rate)喷水量blowdown flow(rate)排污量theoretical air理论空气量excess air ratio过量空气系数hot air temperature热风温度exhaust gas temperature排烟温度theoretical combustion temperature理论燃烧温度adiabatic temperature炉膛出口烟气温度furnace outlet gas temperaturefurnace exit gas temperature汽水阻力pressure dropdraft loss通风阻力pressure drop自生通风压头stack draftavailable static head运动压头circulation ratio循环倍率circulation velocity循环水速steam quality by mass质量含汽率；干度mass velocity质量流速critical steam quality临界含汽率steam quality at minimum heat transfer coefficient 最高壁温处含汽率furnace volume炉膛容积furnace volume heat release rate炉膛容积热负荷heat liberation rate in furnace炉膛截面积热负荷furnace cross-section heat release ratefurnace plan heat release rate燃烧器区域炉壁热负荷burner zone wall heat release ratefurnace wall heat release rate炉壁热负荷furnace wall heat flux density炉壁热流密度critical heat flux density临界热流密度grate heat release rate炉排（面积）热负荷burner heat input燃烧器热功率ignition energy点火能量evaporation rate受热面蒸发率percentage of economizer evaporation省煤器沸腾率primary air一次风secondary air二次风tertiary air三次风imaginary circle假想切圆percentage of air space通风截面比fineness煤粉细度explosion mixture limits爆炸界限furnace炉膛；炉胆fire box火箱smoke box烟箱burner燃烧器tilting burner摆动式燃烧器igniter点火器oil atomizer油雾化器register调风器stabilizer稳燃器wind box风箱burner port燃烧器喷口burner quarl炉排gratehand-fired grate手烧炉排stoker-fired grate机械炉排mechanical stoker链条炉排travelling grate stokerchain grate stoker链带式炉排bar grate stoker横梁式炉排louvre stoker鳞片式炉排vibrating stoker振动炉排inclined reciprocating grate往复炉排spreader stoker抛煤机air compartment风室reinjection system飞灰复燃装置drum锅筒；汽包steam drum上锅筒water drum下锅筒shell锅壳drum internals锅筒内部装置；汽包内部装置steam washer清洗装置cyclone separator旋风分离器turbo separator轴流式分离器baffle plate缝隙挡板corrugated scrubber百叶窗分离器screen separator钢丝网分离器perforated distribution plate多孔板dry pipe集汽管evaporating heating surface蒸发受热面water-cooled wall水冷壁membrane wall膜式水冷壁division wall双面水冷壁anti-clinker box防焦箱gererating tube bank锅炉管束safety valve安全阀safety relief valve安全泄放阀water level indicator水位表injector注水器boiler setting炉墙soot blower吹灰器slag removal equipment除渣设备boiler efficiency锅炉效率；锅炉热效率boiler operating availability锅炉可用率boiler forced outage rate锅炉事故率feed water condition给水品质steam purity蒸汽品质moisture in steam蒸汽湿度boiler water concentration锅水浓度；炉水浓度total dissolved salt总含盐量total solid (matter)全固形物dissolved solid (matter)溶解固形物suspended solid (matter)悬浮物total hardness（总）硬度alkalinity碱度heat loss热损失heat loss due to exhaust gas排烟热损失heat loss due to unburned gases气体（化学）未完全燃烧热损失heat loss due to unburned carbon in refuse固体（机械）未完全燃烧热损失heat loss due to radiation散热损失heat loss due to sensible heat in slag灰渣物理热损失unburned combustible in flue dust飞灰可燃物含量；飞灰含碳量unburned carbon in flue dust炉渣可燃物含量；炉渣含碳量unburned combustible in slagunburned carbon in slag漏煤可燃物含量unburned combustible in siftingdust loading烟气含尘量dust density锅炉负荷调节范围load range of boilerturndown ratio燃烧器调节比air leakage factor漏风系数set pressure整定压力start-to-discharge pressure前泄压力popping pressure起座压力reseating pressure回座压力blowdown回座压差discharge capacity排放量；排汽能力boiler efficiency test锅炉效率试验；锅炉热效率试验hydrostatic test水压试验hydrostatic deformation test验证性水压试验air leakage test漏风试验pressure decay test风压试验load test负荷试验circulation test水循环试验thermal chemical test热化学试验sounding of tube by balls通球试验safety valve operating test安全阀校验flue gas analysis烟气分析Orsat (gas analyser)奥氏（烟气）分析器suction pyrometer抽气式热电偶（高温计）venturi pneumatic pyrometer气力式高温计heat flux meter热流计start-up启动filling上水water level水位initial water level点火水位purge吹扫blowoff放水drain疏水blowdown排污raising pressure升压bringing a boiler onto the line并汽start-up pressure启动压力start-up flow rate启动流量shutdown停炉outage停用out of servicebanking fire压火storage停炉保护chemical cleaning化学清洗boiling-out（碱）煮炉flushing冲管steam-line blowing吹管passivating钝化drying-out烘炉flow stagnation停滞flow reversal倒流separation of two-phase fluid汽水分层steam binding汽塞steam blanketing汽水共腾primingfoaming泡沫共腾external deposit烟气侧沉积物internal deposit汽水侧沉积物slagging结渣fouling积灰clogging堵灰pitting attack点状腐蚀ductile gouging延性腐蚀hydrogen damage氢脆caustic embrittlement苛性脆化high temperature corrosion高温腐蚀low temperature corrosion低温腐蚀overheating超温；过热flashback回火blow off脱火loss of ignition熄火；灭火furnace explosion炉膛爆炸furnace implosion炉膛内爆furnace puff炉膛爆燃blow hole火口secondary combustion二次燃烧Components for CFBC boiler （CFBC锅炉的主要部件）fouling积灰clogging堵灰pitting attack点状腐蚀ductile gouging延性腐蚀hydrogen damage氢脆caustic embrittlement苛性脆化high temperature corrosion高温腐蚀low temperature corrosion低温腐蚀overheating超温；过热flashback回火blow off脱火loss of ignition熄火；灭火furnace explosion炉膛爆炸furnace implosion炉膛内爆furnace puff炉膛爆燃blow hole火口secondary combustion二次燃烧1.parameter/参数rated capacity额定蒸发量nominal capacity最大连续蒸发量maximum continuous ratingrated heating capacity额定供热量nominal steam condition额定蒸汽参数nominal steam parameter额定蒸汽压力nominal steam pressurenominal steam temperature额定蒸汽温度(nominal)hot water temperature热水温度feed water temperature给水温度return water temperature回水温度circulation circuit循环回路steam generating circuit蒸汽净化steam purificationsteam temperature control汽温调节feed water给水condensate凝结水make-up water补给水boiler water锅水，炉水boiling crisis沸腾换热恶化as-fired fuel炉前燃料fire bed,fuel bed火床fire line最高火界additive添加剂flue fas dew point烟气露点Coupling耦合、联轴Couple联轴器CPLCrane起重机Critical临界的Critical speed临界速度Crusher碎渣机Current transformer CT电流互感器Cube立方（体）Cubicle illumination箱内照明Curdle凝固Current电流、当前Cursor光标Curve曲线Custom习惯、海关Custom keys用户键Cutter切削工具Cyanic青色、深蓝色Cycle循环、周期、周波Cymometer频率表Cyclome classifier旋风分离器Cylinder 汽缸CYLD日负荷曲线Daily load curveDaily load日负荷Damage损坏、破坏Damper阻尼器、挡板DMPRDanger危险、危险物Dank潮湿Danger zone危险区Data数据Data base数据库Data acquisition system数据采集系统DASData highway数据高速公路Date日期Data pool数据库Dc lub oil pump直流润滑油泵Dead band死区Deaerator除氧器DEA/DEAE/DEAERDecimeter分米Decrease减少DECDeep深度、深的、深Default默认、缺席Degree度、等级Demand要求、查问Delay延迟Delay time延时Delete删除Demineralized water除盐水Demineralizer除盐装置Deposit沉积结垢Desalt除盐设备Description说明、描述Destination目标、目的地Desuperheater减温器Desuperheater water减温水DSHWTEDetail细节Detect发现、检定Deviate偏离、偏差Device设备、仪器Diagnosis诊断Diagram图形、图表Diagram directory图目录Diagram number图形号Diameter直径Diaphragm膜片、隔板Dielectric介质、绝缘的Diesel generator柴油发电机Difference差异、差别、差额Differential protection差动保护Diff press差压Diff expansion胀差DIFFEXPDifferential pressure差压DP/DSPDigital数字的Digital electric hydraulic电调Digital input/output数字量输入／输出Digital-to-analog数／模转换D/ADioxde二氧化碳Direct current直流（电）DCDirect digital control直接数字控制DDCDisassembly拆卸Disaster事故、故障Disc叶轮Disaster shutdown事故停机Discharge排除、放电、卸载Discharge current放电电流、泄漏电流Disconnector隔离器、隔离开关Disconnect switch隔离开关Discrete input/output离散输入／输出Disk磁盘Disk manage commands磁盘管理命令Dispatch调度、发送派遣Dispatcher调度员Dispatching station调度站（局）Displacement位移Displacement pump活塞泵Display显示、列屏Distance距离Distilled water蒸馏水DISTLWTRDistributed分布\分配\配电（水、汽）Distributed control system集散控制系统DCSDistributed processing unit分布处理单元DPUDistributing board配电盘Distribution network配电网络Distribution substation二次变电站Disturbance扰动Diverter vlv切换线Divided by除以Design设计、发明Division分界、部门Division wall分割屏Documentation文件Door门Dosing pump加药泵Dowel pin定位销Down pipe下降管Download下载Downtime停机时间Dozer推土机Draft通风、草图Drain疏水、排放DRNDrain pump疏水泵Drain tank疏水箱Drawing图样、牵引Drill钻孔、钻头、钻床Drive驱动、强迫Drn collector疏水收集器Drop站Drowned pump潜水泵Drum汽包Drum-type boiled汽包式锅炉Dry干、干燥Dual双重的Duct风道、管道Dust灰尘Dust helmet防尘罩Dust catcher除尘器、吸尘器Duty责任Dynamic动态的Dynamometer功率表E/ Earth大地Earth fault接地故障Earth connector接地线、接地Earth lead接地线、接地Eccentricity偏心、扰度Econ recirc vlv省煤器再循环线Economizer省煤器ECONEdit编辑Efficiency效率Eject pump射水泵Ejection射出Ejector抽气器Electric电的Elbow弯管、弯头Electric-hydraulic control电／液控制Electrical电的、电气的Electrical lockout solenoid vlv电磁阀锁阀Electrical machine电机Electrical service供电Electric power industry电力工业Electrode电极Electric power company电力公司Electric power system电力系统Electronic电子的、电子学的Electrotechnics电工学、电工技术Electrostaic precipitator静电除尘器Electrostatic静电的Element元件、零件、单元Elevation标高ELEVElevator升降机Ellipse椭圆Emergency decree安规Emerg lub oil事故润滑油Emerg off事故停／关闭Emerg seal oil事故密封油Emergency紧急事故EMERGEmergency drain事故疏水Emergency governet／intercepter危急遮断器Employee雇员Empty排空Enclosure外壳、包围End末端、终结End cover端盖Energize激励、加电Energy能、能量Energy meter电度表Energy source能源Engineer keyboard工程师键盘Engineer station工程师站Engineer's console工程师操作站Engineering工程Enter开始、使进入Entry输入Equalizer valve平衡线Equipment设备Erase删除Error错误Escape valve安全线Evaporate蒸发、冷化Evaporating蒸发量Event事件Excess超过、过度Excess combustion air过剩燃烧空气Excitation励磁Exciter励磁机Exhaust排汽EXHExhaust portion排汽段Exit出口Expansion/ EXP膨胀Expansion tank扩容箱Expenditure费用Expert专家、能手Explosion爆炸Exponent指数幂External外部的、表面的。

用英文介绍锅炉的作文

用英文介绍锅炉的作文A boiler is a device that is used to heat water or generate steam for various purposes. It plays a crucial role in many industries and households, providing heat and hot water for various applications. In this article, we will explore the functions, types, and working principles of boilers.Boilers serve a wide range of purposes, from heating buildings to powering industrial processes. They are commonly used in residential homes, commercial buildings, and industrial facilities. The primary function of a boiler is to transfer heat energy from a fuel source to water, which is then circulated to provide heat or generate steam.There are several types of boilers, each designed for specific applications. The most common types include:1. Fire-tube boilers: These boilers have a cylindrical shell filled with water, and hot gases pass through tubes located inside the shell. The heat from the gases is transferred to the water, generating steam.2. Water-tube boilers: In these boilers, water circulates through tubes that are surrounded by hot gases. The heat is transferred to the water, producing steam. Water-tube boilers are commonly used in power plants and large industrial settings.3. Electric boilers: These boilers use electricity as the fuel source to heat water or generate steam. They are often used in residential homes and small-scale applications.4. Biomass boilers: These boilers use organic materials, such as wood pellets or agricultural waste, as the fuel source. They are considered environmentally friendly and are commonly used in rural areas.The working principle of a boiler involves the combustion of a fuel source, which produces heat. This heat is transferred to the water or surrounding medium, resulting in the production of steam or hot water. The combustion process is typically facilitated by aburner, which ignites the fuel and creates a flame. The heat generated by the flame is then transferred to the water or tubes, raising its temperature.Boilers are equipped with various components to ensure their safe and efficient operation. These components include:1. Burner: The burner is responsible for igniting the fuel and creating a flame.2. Heat exchanger: The heat exchanger facilitates the transfer of heat from the combustion process to the water or surrounding medium.3. Control system: The control system regulates the operation of the boiler, ensuring optimal performance and safety.4. Safety valves: Safety valves are designed to release excess pressure to prevent explosions or other hazardous situations.In conclusion, boilers are essential devices used for heating and generating steam. They come in various types, each designed for specific applications. The working principle involves the combustion of a fuel source, which transfers heat to the water or surrounding medium. Boilers are equipped with components to ensure safe and efficient operation. Understanding the functions, types, and working principles of boilers is crucial for anyone working with or relying on these devices.。

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锅炉系统1 冷凝器1.1 简介欧堡生产的冷凝器是用直管和一个外部密封浮头组成的管壳式冷凝器。

这种冷凝器主要用作废气锅炉，蒸汽加热或洗舱海水加热器的转储冷凝器/冷却器排水。

并取得权威船级社批准。

温度计，排水阀，空气阀，压力表的安装设计为½“BSP内螺纹安装。

这些组件可能是指定的。

而蒸汽或水的控制设备是可选的。

1.2 安装空间要求安装时必须有足够的空间供作清洗，检查或更换管的插入与撤出。

冷凝器必须安置在水平并稳定的表面。

1.3 存储如果冷凝器在安装前要闲置一段时间，应存放在干燥的储藏室里。

如果储藏室潮湿，冷凝器必须放在装有硅胶的包装袋子里。

为了避免破坏，建议冷凝器放在原包装中。

冷凝器已经在交付前做过液压试验。

试验中所用测试媒质含有一定的数额抗腐蚀保护物质。

当冷凝器需闲置的时间较长，建议使用指定产品作为防腐蚀物质1.4 安装冷凝器设计为垂直或水平安装。

在水平安装的情况下，蒸汽喷嘴必须朝上，而冷凝水出口喷嘴朝下。

如果是垂直安装冷凝器，蒸汽入口和海水出口端必须朝上。

排水和空气排放阀必须安装在冷凝器在最低和最高点的中间线的位置。

任何选择性的控制设备必须根据具体指示安装。

步骤A：将冷凝器安装在水平平面上。

步骤B：钻基础固定螺栓孔。

步骤C：将螺栓放入孔中并拧紧。

连接冷凝器步骤D：移除所有的塞子和盲板，然后再连接冷凝器。

步骤E：在连接中确保没有杂质进入。

步骤F：管道连接起来，确保从管道和冷凝器之间没有强制力的产生。

1.5 调试启动前要确保所有连接都牢固地拧紧是很重要的。

同样重要的是，冷凝器和连接管道空气要彻底排出。

步骤A：如果装有安全阀，必须加以调整到最大设计压力或较低。

步骤B：法兰螺栓要拧紧。

拧紧法兰螺栓时始终使用扭矩扳手。

步骤C：运行一小时，停止冷凝器，并重新拧紧所有螺栓。

步骤D：启动阶段，冷凝器的两边都要排出空气，必须认真仔细的检查回路的泄漏。

1.6 性能冷凝器性能须附和传热计算表规定的要求。

，保持指定的蒸汽压力特别重要，因为压力降低可能导致进口速度过大，将会使其产生噪音并损害冷凝器，而较低的压力下会降低热性能。

通常，有效评估冷凝器性能的方法是通过监测评估冷凝水出口温度或海水出口温度。

如果冷凝水温度过高或海水出口温度过低，要么是冷凝器需要清洗或操作参数不正确。

需要检查其工作条件，并采取适当的纠正行动，以使性能恢复所要求的水平。

1.7 在关闭期间的保护在关闭期间发生的腐蚀，主要是由于氧气的存在。

如果存在非蒸馏水，如碱性或海水在冷凝器中，就很容易发生腐蚀。

然而，即使在完全放空的情况下，冷凝器接触到残留的冷凝水仍然会造成腐蚀。

因此，当停止工作时，应当通过使用淡水冲洗海水端，并仔细在两端泄放以保护冷凝器，如果冷凝器需在一个较长时期的停止工作，尤其是在寒冷的冬季。

必须小心清空。

打开空气阀口并检查堵塞情况。

1.8 维护和清洁冷凝器应定期清理，每十二个月或当没有其他原因的情况下而输出下降的时候，应将内部的管子移出清洁。

步骤A：检查是否有水在收集箱或管子中。

步骤B：将内部管束取出后，用有压力的液体进行外部清洗步骤3：将管束的上盖移除后，使用酸性的液体从内部进行清洁，表面的杂质可以用软质尼龙刷去除。

但很重要的一点是进行机械清除时不要破坏管子的表面。

步骤D：安全阀必须每年都要检查其设置点是否正确。

1.9 拆卸和重装管束当需要将管束从冷凝器中取出时，必须拆除海水连接头，拆下蒸汽进口处的水箱，松下其他水箱的连接螺栓需要利用水箱中的顶升螺栓将水箱和管架连接用的紧固O形圈拉开。

在拉出管束前，应使用带状材料缠绕保护管架箱浮动端的表面。

由于管束和包装表面容易损伤，一定要轻拿轻放。

检查管束，水箱和外壳是否遭到破坏或过度磨损，进行必要的维修和清洗后，重新组装冷凝器。

在水箱浮动端的环槽中安装新的O形圈，并涂耐热硅润滑脂，使安装更容易，并可以增加垫材的使用寿命。

然后将管束装入管架中，在插入管束前，管架始终要用包装材料保护。

使抗冲击板块正对蒸汽喷嘴的冲击是十分重要的，不然可能会因为管子被过度侵蚀而发生故障。

安装末端水箱。

取下管架浮动端的包装带，轻轻地将浮动端水箱滑上。

这是极为重要的板块正面临冲击的蒸汽喷嘴，否则可能会失败，使用法兰螺栓确保无偏斜地固定水箱后，装上管子并锁紧螺丝。

垫片表面要清洁并防止损坏，每拆下一个接头都要更换新的垫片。

应当尽量使用原装垫片和垫圈，并保证安装牢固紧密。

需始终使用扭力扳手上紧法兰螺栓。

运行冷凝器一个小时，停止，然后上紧法兰螺栓。

对接头的紧密性进行压力实验。

在运行期间，对冷凝器进行小心的泄放，并对循环回路进行检查是否漏泄。

1.10 备件订货时请注明零件的冷凝器（在铭牌上）的序列号。

需要备件的进一步信息，请联系欧堡工业。

2 化学定量泵2.1 简介化学定量泵是由微处理器控制的电磁定量泵。

该泵能够准确显示液体化学品加药压力管道系统中的流量，并能进行容器的打开和关闭。

化学定量泵的主要组成部分包括操作面板，电源端，液源腔该泵的工作原理是液端定量膜由微处理器控制作动的电磁铁驱动，形成脉冲作用在化学液体上，这就引起吸口端，液体腔和排出端之间产生压力差。

这个压力差将引起吸口和出口的自动阀开启或关闭，从而供应化学液体。

泵的容量（供给速度）取决于行程长度和行程率。

冲程长度使用行程长度调节旋钮在0％和100％间调节。

最佳剂量是设置在30％和100％行程的长度。

行程率10%和100％之间使用的多功能开关进行步进调节，每级为10%。

但在外部模式中，行程率是由电信号控制的。

2.2 安全在安装，调试，运行，维护和修理期间必须始终应遵守遵循以下安全原则请注意，泵的设计不适合用于：（1）气体化学物质或悬浮固体和容易爆炸的危险场所。

（2）在紧急情况下的泵应立即关闭。

断开电源的电源线。

（3）在任何时候都应该能够方便地进行操作和管理。

附近不能有障碍（4）水泵和外围设备只有合格和有授权的维修人员才能对其进行维修和管理。

（5）当做有关泵的工作时，首先要断开电源（6）在做有关泵的工作前，必须泄放出口管路上的压力液体，放空液腔中的液体，并冲洗干净。

（7）务必阅读化学品安全数据。

（8）处理危险或未知的化学物质，务必穿上防护服时（9）如果排出管被封锁，切勿让定量泵运转，因为这可能会导致排出管道破裂。

2.3 安装2.3.1 一般安装化学定量泵通常预装在化工罐上。

因此该泵安装或更换的地方必须遵守以下安装注意事项：（1）化学定量泵必须位于一个环境温度在-10 C至+45之间，在非冷凝的情况下相对湿度不超过92%的环境中（2）泵的泵脚必须牢固地安装在牢固的基准座上，泵运行时不能震动（3）启动和运行时不得超过其最大允许压力。

这种泵的最大吸高为2 mmWC，最大工作压力为16巴。

例如由于化学物质供应系统的位置，导致运行压力超标的情况下，在出口端必须安装一个安全阀，多余的液体回到吸口（4）吸入和排出阀必须安装在垂直位置。

（5）其管子必须具备这样的要求，即如果需要，允许将泵和液腔拆开，在安装时不能产生应力和弯曲，所以只有原装的产品才能达到这种尺寸要求。

（6）吸入管应呈上升趋势并尽可能短以防止气泡的形成。

（7）由于在底部有化学品的沉淀和杂质，底阀的位置要高于它们的位置。

（8）连接到供应系统的出口管的止回阀必须上紧。

2.3.2 电气安装该泵是和主电源的连接通过主电源线。

如果泵连接到电源时与感应元件并联，必须对他们进行电器隔离，防止开关断开时产生的冲击造成损害。

2.4 操作这个化学定量泵的操作面板配有支持泵的设置和运作操作开关，接线端子，和指示器。

该泵可通过手动操作控制或外部控制。

如果泵仅需要手动操作模式时将不会提供可选的终端接到“外部控制”。

当泵需要是通过“外部控制”和/或“浮动开关”控制时，必须提供可选的终端外部控制。

“在化学品罐中装有测量液位的浮动开关，它能够提供液位信号到泵。

由于液位的变化需要安装两个浮动开关到接线端子。

同时泵也需要进一步安装故障监测继电器用于低水位报警。

以下为泵操作指令的完整描述。

如果化学计量泵包括零件或功能，不是用于定量供应系统，这些指令可以忽略。

2.5 泵的基本信息2.5.1 行程长度调节旋钮行程长度可以在0％和100通过调节冲程长度调节旋钮进行连续性的调节。

在技术上只有再现性在调整范围30％至100％可行。

2.5.2 多功能开关多功能开关用来选择操作模式和设置行程率。

下面的操作模式是供多功能开关选择的模式：停止。

外部。

手动（设置在10％的行程步进率）。

测试（自吸功能）。

（1）停止“停止”功能使泵电源未断开也可以停用。

（2）外部外部操作模式允许通过触点或者半导体的外部模式操纵设备单独调节其行程“暂停”功能，可以通过外部终端远程操作使泵停止。

（3）手动操作手动操作模式通过多功能开关对行程率进行10％的步进调整。

（4）测试“测试”功能检查泵的自吸的功能。

开关设置在测试位时，多功能开关“测试”是自动的。

2.5.3 LED指示灯运行和错误状态通过操作面板上的三个指示灯显示：绿色LED指示灯，操作显示：此LED点亮时排出行程被激活。

黄色的LED指示灯，报警指示灯：如果设备装有浮动开关，LED灯亮时，表明液面低于第一触发液面。

红色LED指示灯，故障指示灯：如果装有浮子开关，指示灯亮起来时说明液位测量发生故障。

它闪烁时表示未定义的运行状态2.6 保养.为确保化学定量泵工作安全和性能可靠，必须进行定期保养。

正常保养间隔为三个月。

这是根据其运行时间大约为30％时制定的。

但在使用比较频繁的情况下，保养周期应缩短。

进行以下维护工作：检查泵短期运行时进给率是否正确。

检查排气孔处的化学品是否渗流。

检查排出管与液源端连接是否牢固。

检查排出和吸入阀是否牢固地固定。

检查液源端尤其是排气孔处的水密性。

检查膜片是否损坏检查液源端的固定螺丝是否上紧。

检查泄放阀是否牢牢地固定到位。

检查泄放功能是否正常运行。

检查电气接线有没有破损。

Boiler System1 Condenser1.1 General descriptionAalborg Industries' MD condensers are of the shell and tube type with straight tubes and an externally sealed floating head. The MD condenser is primarily used as dump condenser/drain cooler for exhaust gas boilers, or as steam heated tank cleaning heater for sea water. The condensers are approved by major marine classification societies.Thermometers, drain valve, air valve, and pressure gauge can be fitted on designated ½" BSP threads. These components may be supplied on request. Control equipment for either steam or water is optional.1.2 Installation space requirementsWhen mounting the condenser sufficient space must be allowed for withdrawal of the tube insert for cleaning, inspection, or replacement purposes. The condenser must be placed on a level and stable surface.1.3 StorageIf the condenser must be stored prior to the installation, it should be in a dry storage room. If the storage room is damp, the condenser must be wrapped together with bags of silica gel. To avoid damages it is recommend that the condenser is stored in the original packing.The condenser has been hydrostatically tested before delivery. The used test medium contains a certain amount of corrosion protection .When the condenser is kept in storage for an extended period of time, it is recommend to use Castrol Rustilo Aqua 2 as protection against corrosion.1.4 installationThe condenser is designed for either vertical or horizontal installation. In case of horizontal installation the steam inlet nozzle must face upwards, and the condensate outlet nozzle face downwards.If the condenser is mounted vertically, the steam inlet and sea water outlet end must face upwards. Drain and air vent valves must be mounted according to the orientations of the condenser e.g. lowest and highest ½" thread position on the shell.Any optional control equipment must always be installed according to specific instructions.STEP A：Place the condenser on a level and plane surface.STEP B：Drill the holes for the foundation bolts.STEP C：Place the bolts into the holes and tighten up.Connecting the condenserSTEP D：Remove all plugs and blind flanges before connecting the condenser.STEP E：Ensure that no impurities are present in the connectionSTEP F：Set up the pipe connections and make sure that no forces from the piping are transferred to the condenser1.5 CommissioningBefore start-up it is important to make sure that all connections are securely tightened. It is equally important that the condenser and the connecting pipes are thoroughly air-vented.STEP A：If a safety valve is fitted it must be adjusted to maximum design pressure or lower.STEP B：Tighten all main flange bolts . Always use a torque wrench when tightening the flange bolts.STEP C：Operate the condenser for one hour, stop, and retighten all bolts .STEP D：Both sides of the condenser must be carefully vented and the circuits carefully inspected for leakage during the whole start-up period.1.6 PerformanceThe performance of the condenser is subject to the conditions specified in the heat transfer calculation sheet. It is particularly important that the steam pressure is maintained as specified, since lowering the pressure may cause excessive inlet velocity which may be both noisy and harmful to the condenser, as well as the lower pressure will decrease the thermal performance. Usually it will be sufficient to evaluate the performance of the condenser by monitoring the outlet temperature of either the condensate or the water outlet temperature . If the condensate temperature is too high or the sea water outlet temperature is too low, either the condenser needs cleaning or the operating parameters are incorrect. Check the operating conditions and take appropriate corrective action to bring the performance back to the required level.1.7 Conservation during shut down periodsCorrosion occurrences in shut down periods are mainly caused by oxygen. The corrosion occurs if non-distilled, alkaline or sea water remains in the condenser. However, even when fully emptied, the condenser is exposed to corrosion caused by water residues or condensation. Hence, when out of service, it should be protected against corrosion by flushing with fresh water on the sea water side and carefully draining of both sides.If the condenser is out of service for an extended period of time – in particular during winter seasons with frost – it must be carefully emptied. Open the air vent valve and check for clogging.1.8 Maintenance and cleaningThe condenser should be cleaned regularly by removing the tube insert every twelve months or at any time there is a decrease in output not related to other causes.STEP A：Check if any deposits have collected in the water boxes or in/on the tubes.STEP B：Cleaning of the tube bundle from the outside is carried out after removing the tube insert using a liquid jetSTEP C：Cleaning of the tube bundle from the inside is carried out after removing the cover by flushing the tubes with e.g. citric acid. To remove scales or impurities asoft nylon brush can be used, but it is very important not to damage the tube surface during mechanical cleaning.STEP D：Once every year the safety valve must be checked for correct set point.1.9 Dismantling and reassembling of the tube bundleWhen the tube bundle must be pulled from the condenser, the sea water connections must be dismantled and the water boxes at the steam inlet removed. Loosen the bolts for the other water box and use the jacking bolts in the water box to pull the water box off the tight O-ring fitting with the tube sheet. Protect the floating end tube sheet packing surface with a wrap of tape before pulling the bundle. Handle the bundle and water boxes with care, since both tubes and packing surfaces can be damaged by impact.Inspect the tube bundle, water boxes and the shell for damage and excessive wear, make necessary repairs and cleaning and reassemble the condenser. Fit new O-rings to the floating end water box gasket grooves and grease with heat resistant silicone grease to ease the mounting and increase the gasket life time. Mount the bundle in the shell and remember to protect the packing surface of the tube sheet before inserting the bundle. It is extremely important that the impingement plate is facing the steam inlet nozzle, otherwise the tubes may fail prematurely due to erosion. Mount the fixed end water box. Remove the protective tape from the floating end tube sheet and gently slide the floating head water box on. Use the flange bolts to ensure a proper fitting without yawing of the water box. Set up the piping again and tighten all bolts.Gasket surfaces must be cleaned and protected against damage. New gaskets should be fitted every time a connection has been dismantled. To ensure a tight fit only original spares should be used when replacing the gaskets and O-rings.Always use a torque wrench when tightening the flange bolts.Operate the condenser for one hour, stop, and retighten all boltsA pressure test should be carried out to prove tight joints.Both sides of the condenser must be carefully vented and the circuits carefully inspected for leakage during the whole start-up period.1.10 Spare partsWhen ordering spare parts please state the serial number of the condenser (located on the nameplate). For spare parts and further information please contact Aalborg Industries.2 Chemical dosing pump2.1 GeneralThe chemical dosing pump is a microprocessor controlled solenoid metering pump. The pump offers highly accurate reproducible metering in the dosing of liquidchemicals in pressurised pipe systems, and into open and closed containers. The main components of the chemical dosing pump are the operating panel, power end, and liquid end..The working principle of the pump is that chemical feed occurs as a result of pulsed deflections of the dosing diaphragm within the liquid end, which causes pressure differentiation between the suction side, liquid end cavity, and discharge side. The pressure differentiation causes the suction and discharge self-acting valves to open and close, resulting in chemical feed. The dosing diaphragm is driven by an electromagnet, which is stimulated and controlled by a microprocessor.The pump capacity (feed rate) is determined by the stroke length and stroke rate. The stroke length is set between 0% and 100% using the stroke length adjustment knob. Optimum dosing reproducibility is achieved by setting the stroke length between 30% and 100%. The stroke rate adjustable in 10% steps between 0% and 100% using the multifunction switch. However, in "external" operating mode the stroke rate is controlled by electrical signals.2.2 SafetyThe following safety guide lines must always be observed during installation, commissioning, operation, maintenance, and repair:（1）Please note that the pump is not designed for:Use with gaseous chemicals or suspended solids and in explosion-hazardous locations.（2）In emergency cases the pump should be switched off immediately. Disconnect the power cable from the power supply.（3）The pump must be accessible at all times for both operation and servicing. Access must not be obstructed in any way.（4）The pumps and peripherals must be serviced and repaired by qualified and authorised persons only.（5）Before working on a pump always disconnect the mains power.（6）Before working on a pump always de-pressurise the discharge line, empty the liquid end, and rinse out.（7）Always read the chemical safety data.（8）Always wear protective clothing when handling hazardous or unknown chemicals.（9）Never allow the metering pump to operate if the discharge line is blocked, as this can result in a rupture of the discharge line.2.3 Installation2.3.1 general InstallationThe chemical dosing pump is normally pre-mounted a chemical tank. However, in case that the pump must be mounted elsewhere or replaced please observe the following general installation notes（1）The chemical dosing pump must be located in an environment with ambient temperature between -10︒C to +45︒C and a maximum permissible relative humidity of 92% non-condensing.（2）The pump must be mounted with the pump foot resting on a firm horizontal base. Ensure that it is fastened into place firmly, and will not vibrate in operation.（3）The maximum permissible priming and operating pressures must not be exceeded. For this type of pump the maximum priming lift is 2 mmWC and the maximum operating pressure is 16 barg. In case that the operating pressure is exceeded, e.g. due to the position of the chemical feed into the feed system, the discharge side must be provided with a relief valve. The surplus chemicals should be led back to the chemical tank.（4）Suction and discharge valves must be installed in a vertical position.（5）The tubing should be attached in such a way that it allows lateral detachment of the pump and liquid end, if necessary. The tubing must be free from stress and bends when fitted. Only original hoses with the correct dimensions should be used.（6）The suction tubing should be as short as possible and rising in order to prevent air bubbles forming.（7）The foot valve should be installed so that it hangs just above the bottom of the chemical tank. For chemicals with impurities or sedimentation at the bottom, the foot valve should be positioned well above this layer.（8）The check valve, which connects the discharge line to the feed water system, must be tightened properly.2.3.2 Electrical installationThe pump is connected to the mains power supply by using the mains lead. If the pump is connected to the mains in parallel with inductive power consumers (e.g. solenoid valves, motors) it must be electrically isolated. This prevents damage caused by induction and voltage surges when switching off. illustrates the power element of the pump.2.4 operationThe operation panel of the chemical dosing pump is equipped with operation knobs/switches, connection terminals, and indicators, which support the operation and setting of the pump.The pump can be operated through manual control or external control. If the pump is intended only to operate in manual mode it will not be provided with the optional terminal connection "external control" 。

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