基于全控型电力电子器件的强制换流型混合直流断路器

基于全控型电力电子器件的强制换流型混合直流断路器,在辅助换流电路分断过程中,缓冲电容放电会影响机械开关分断时间;当主断路器完成分断动作,线路能量仅仅依靠避雷器释放,避雷器投入费用较高,能量释放过程较慢,容易造成器件损坏,并影响避雷器使用寿命。提出一种强制换流型混合直流断路器方案,分析了该断路器工作原理,通过对比仿真验证了该方案的可行性。与传统基于全控型器件的强制换流型混合断路器相比,其在实现电流双向流动的同时全控型器件减半;阻止了缓冲电容放电对机械开关动作时间的影响;引入接地引流二极管,可使线路电流尽快减少到零。

一种强制换流型混合式高压直流断路器方案

高压直流断路器在直流系统保护中起着重要作用。针对现有直流断路器在经济性、合闸电弧问题和快速性方面不能兼备的缺陷,提出了一种强制换流型混合式高压直流断路器拓扑。所提方案的拓扑结构中引入了1个绝缘栅双极晶体管(insulated gate bipolar transistor,IGBT),用来配合隔离开关进行合闸操作;引入二极管组并将平波电抗器均分在断路器两侧,以减小对避雷器的压力,延长避雷器的使用寿命;电力电子支路用子模块级联拓扑,避开了大规模IGBT动态均压的技术难题。基于所提拓扑设计了10kV直流断路器,对正常运行以及故障切除、故障恢复合闸下的运行情况进行了分析及仿真,同时与含ABB方案的两种典型方案进行了比较。仿真结果表明:基于所提拓扑的直流断路器最快切除故障电流时间为3.63 ms,开断电流容量为4.09 kA,正常合闸机械支路端电压为0,实现了无弧合闸,IGBT使用数量较ABB方案减半,避雷器吸收能量较传统方案减半,经济性较好,符合直流断路器性能要求。该结果验证了所提拓扑结构具备可行性。

一种强制换流型混合直流断路器方案

作为高压直流输电的关键设备之一,直流断路器受到了广泛的关注。混合直流断路器继承了机械断路器通态损耗低与固态断路器开断迅速的特点,是目前直流断路器研究的主要方向。文中着重分析了影响基于全控型电力电子器件的强制换流型混合直流断路器开断速度的因素,针对辅助换流电路中缓冲电容放电回流影响机械断路器动作时间以及能量吸收电路吸收能量的时间问题,提出一种强制换流型混合断路器方案,该方案能够防止缓冲电容电流回流,同时减少避雷器吸收能量所用时间。对该断路器各个工作阶段的数学模型进行了数值分析,通过Pscad/EMTDC软件对故障状态混合断路器开断过程进行仿真,并且与典型强制混合直流断路器开断过程进行比较,验证了该方案切实可行。

换流变阀侧套管水冷散热设计与优化分析

随着我国输电线路输送容量的提升,换流变阀侧套管的发热问题日益严重,为提升其长期运行可靠性,该文提出一种适用于换流变阀侧套管的强制水冷结构。采用三维电磁–热–流耦合方法对该结构套管温度分布进行仿真分析,并通过温升试验验证其冷却效果。仿真与试验结果表明,加入水冷结构后,套管内部温度下降明显,且当空气间隙为3mm、冷却水温为45℃时,温度对芯体电场影响最小。研究表明,强制水冷结构能有效解决套管发热问题,进而提高套管载流能力与运行可靠性。

Experimental Study of Fouling on Heat Transfer Surface During Forced Convective Heat Transfer

An experimental study was conducted to investigate the fouling process of calcium carbonate on the heat transfer surface, during forced convective heat transfer. The dynamic monitoring apparatus of fouling resistance was set up for the present experiments. The fouling behavio（s were examined under different factors including fluid velocity, hardness,alkalinity, solution temperature, and wall temperature. Asymptotic fouling curves varying with time were obtained. The fouling rate and asymptotic fouling resistance increased and the induction periods were shortened with the fluid velocity decreasing, hardness andalkalinity increasing, and solution temperature and heat transfer surface temperature increasing. Thecomponents of fouling that formed on the heat transfer surface included crystallization fouling and particulate fouling. The thermal performance parameter of fouling,ρfhf, varied from 380 to 2600 kg·W·（m^4·K）^-1, increasing with growing velocity and decreasing solution temperature, hardness or alkalinity. Furthermore, the thermal conductivity of fouling, λf, varied from 1.7 to 2.2 W·（m·K）^-1 .

Turbulent forced convection in a heat exchanger square channel with wavy-ribs vortex generator

Turbulent forced convective heat transfer and flow con figurations in a square channel with wavy-ribs inserted diagonally are examined numerically. The in fluences of the 30° and 45° flow attack angles for wavy-ribs, blockage ratio, R B= b/H = 0.05–0.25 with single pitch ratio, R P= P/H = 1 are investigated for the Reynolds number based on the hydraulic diameter of the square channel, Re = 3000–20000. The use of the wavy-ribs, which inserted diagonal in the square channel, is aimed to help to improve the thermal performance in heat exchange systems.The finite volume method and SIMPLE algorithm are applied to the present numerical simulation. The results are presented on the periodic flow and heat transfer pro files, flow con figurations, heat transfer characteristics and the performance evaluations. The mathematical results reveal that the use of wavy-ribs leads to a higher heat transfer rate and friction loss over the smooth channel. The heat transfer enhancements are around 1.97–5.14 and 2.04–5.27 times over the smooth channel for 30° and 45° attack angles, respectively. However, the corresponding friction loss values for 30° and 45° are around 4.26–86.55 and 5.03–97.98 times higher than the smooth square channel, respectively. The optimum thermal enhancement factor on both cases is found at R B= 0.10 and the lowest Reynolds number, Re = 3000, to be about 1.47 and 1.52, respectively, for 30° and 45° wavy-ribs.

Forced Convective Heat Transfer Experiment of Supercritical Water in Different Diameter of Tubes

Forced convective experiment of supercritical water was performed in Inconel-625 tubes of 4.62 mm, 7.98 mm and 10.89 mm in diameter. The water flowed upward, covering the ranges of pressure of 23.4 MPa to 25.8 MPa, mass flux of 90 kg/m^2s to 3,281 kg/m^2s, local bulk temperature of 102-384 ℃, inner wall temperature of 167-669℃ and heat flux of up to 2.41 MW/m^2. The results exhibited severe deteriorated and enhancement heat transfer. The experimental results can be calculated by the Jackson＇s correlation and the Bishop＇s correlation mostly. But some data with strong effects of the buoyancy force and the variations of flow regimes can not be predicted properly.

Forced-Flow Convection for Liquid Methanol Flowing through Microchannels

Experiments were conducted to investigate the single phase forced-flow convection of methanol flowing through microchannels with rectangular cross-section.The fully-developed turbulent convection regime was found to be initiated at about Re=1000-1500,The fully developed turbulent heat transfer can be predicted by the well-known Dittus-Boelter correlation with mere modification of the original empirical constant coefficient 0.023 to 0.00805.The transition and laminar heat transfer behaviors in microchannels are highly peculiar and complicated,and heavily affected by liquid temperature,velocity and microchannel size.

Airside fin efficiencies for finned-tube heat exchangers with forced convection

The heat transfer and mass transfer fin efficiencies were analyzed numerically to show that popular models for heat transfer fm efficiency for circular fins are not always reasonable. The numerical results show that the effective heat transfer area of a circular fin increases several times faster than that of a straight fin for the same tube radius. Then, a simple but accurate heat transfer fin efficiency model was developed and verified by numerical results for a wide range of fin designs. This model predicts the heat transfer fin efficiency with absolute errors of less than 1%. The heat transfer and mass transfer fin efficiencies were found to be quite different for typical air flow with low relative humidity. Thus, these two fin efficiencies should not be assumed to be equal and a mass transfer fin efficiency model was developed, based on the heat transfer fin efficiency model. These heat transfer and mass transfer fin efficiencies are very useful for more accurate prediction for a wide range of practical applications.