进口弯头对分配集箱流量分配影响的试验研究

进口弯头对分配集箱中的流量分配有较大的影响。为此，针对1台锅炉中其分配集箱带弯头入口的顶棚管过热器受热面管流量分配做了较详细的试验研究。研究发现，弯头上不同区域的管产生不同的流量偏差，并且弯头出口附近直管集箱上的管中流量也会受弯头的影响。最后，根据试验分析得到的产生流量偏差的原因和特点，提出了消除流量偏差和解决爆管的措施。     

电站锅炉三通集箱流场的数值研究

根据电站锅炉三通集箱系统的结构特点,采用基于三维实体模型的建模方案,对径向引入引出集箱系统的流场分布进行了数值模拟。采用FLUENT软件分析了集箱流场的分布特点及受热面沿程阻力对集箱速度、静压分布的影响,详细讨论了三通结构、受热面沿程阻力对受热面流量分配的影响。研究结果表明,集箱流场呈三维分布,分为径向引入管下游的冲击射流区和周围的强迫对流区,三通结构直接影响集箱的速度分布;受热面的流量分配直接受三通结构的影响,沿程阻力影响受热面流量偏差的大小。     

管组集箱采用三通结构引入引出对锅炉再热器热偏差的影响

再热器蒸汽侧压降一般很小,集箱中的静压分布将是决定并联管屏流量分配的重要因素.当集箱引入管为三通结构时,在三通区域的集箱中存在涡流区,使该区域的集箱静压大大下降,造成这部分管屏流量偏小,热偏差增大,甚至导致超温爆管.本文根据实炉再热器的出口汽温分布特征,以及三通管流场和静压分布的实验结果,分析了屏间热偏差产生的原因,并提出减小屏间热偏差的改进方向.     

三通集箱过热器压力分布与流量分配的数值模拟

为了解三通结构对过热器流量分配的影响从而解决三通集箱过热器的爆管问题,利用Fluent软件对过热器模型进行了数值模拟,研究了三通结构集箱过热器内的静压分布、速度分布、各支管流量分配及各支管入口处流体的流速分布和静压分布.结果表明:三通结构附近流体的压力低且速度大,而远离该区域的流体则压力高且速度小;三通中涡流区域的支管入口有小涡流,而其他区域的支管入口没有出现小涡流;集箱内涡流下部的支管流量偏小,正对集箱入口处的支管流量最大;将第7管屏和第11管屏的入口形状改为圆形,改造后支管的流量明显增大.     

直流锅炉双相流体管组的热偏差

直流锅炉等蒸发受热面一般都是由许多根管子并联组成的,由于各管的长度、弯头、内径等结构尺寸不同,进出口集箱中沿集箱长度静压变化的影响,以及各管受热情况不同,使各管出口处工质的焓不同,这就是热偏差现象。本文首先讨论了以平均管的压降代替管组压降的可靠性,因为一般在手工计算中是用平均管的压降与偏差管的压降相平衡的原则来计算热偏差的,分析指出在压力较高,     

135 MW CFB锅炉L形屏式过热器热偏差分析

以一台135 MW CFB锅炉的L形屏式过热器为例,对其热偏差产生机理进行了研究。通过建立热偏差计算模型和自主编制的软件,计算和分析了其同屏及屏间热偏差系数。结果表明:在同屏管组的引入引出管采用Z形布置时,集箱效应与管组内外侧管长结构不均匀对流量分配的影响相互抵消,达到了流量均匀分配的效果,同屏热偏差主要受结构不均匀和热负荷分布的影响;在各管组引入引出管的进出口集箱采用Z形布置时,由于集箱效应,屏间流量分配明显不均,这是造成屏间热偏差的主因;在实际应用中,应充分利用集箱效应对屏内及屏间工质流量分配的影响,使管内工质流量分配与管外热负荷分布相互配合,达到控制屏式过热器热偏差的目的。     

超临界压力下水冷壁中间集箱分配特性的研究

研究了国产600 MW直流锅炉分配集箱水冷壁管在超临界压力下的流量分配特性。试验参数为:压力p=23~25MPa,质量流速G=400~1 200 kg/(m2.s),工质温度t=10~400℃。试验研究了工质压力、质量流速和工质温度对分配集箱垂直水冷壁管流量分配特性的影响。试验结果表明:随着质量流速的增加,垂直水冷壁管间流量分配的均匀性增加;在拟临界点附近,流量分配不均匀性有一阶跃增加,而且随着压力的增加,流量分配不均匀性在拟临界点的阶跃增加现象变弱。利用分配集箱并联支管的离散模型计算了分配集箱垂直水冷壁管内的流量分配,计算结果与试验数据吻合。     

电站锅炉过热器、再热器集箱静压分布的数值研究

利用数值模拟的方法，研究了径向引入引出型分配、汇流集箱系统的静压分布规律。为了消除计算中伪扩散的影响，选用了QUICK格式。数值计算结果表明：在三通附近，气流的变化非常强烈，在远离三通的区域．气流逐渐平稳。在分配集箱进口三通的两侧存在2个涡流区，正对三通中心线的支管处静压最高，远离三通的区域，静压分布与轴向引入引出方式规律基本一致。利用该方法计算了某电厂锅炉末级再热器的流量分配和热偏差情况，与实测结果相吻合。图6表1参2     

T型进口三通对分配集箱流量分配的影响

Ｔ型进口三通的布置方式分配集箱中的流量分配有着严重的影响。该文对三通附近涡流区中的集箱静压分布和支管入口阻力系数进行了深入的实验研究。     

应用旋流器控制并联管组中流量分配的实验研究

在分配集箱的进口处加装一只旋流器,使进入集箱中的流体发生旋转,增加沿程摩擦阻力对集箱静压分布的影响,从而达到控制并联管组流量分配的目的。在旋流条件下所得出的离散型数学模型,能够预测不同旋流强度下的集箱静压分布和管流量分配,计算值和实验结果吻合良好。图１０参６     

MASS FLOW RATE DISTRIBUTION AND PHASE SEPARATION OF R-22 IN MULTI-MICROCHANNEL TUBES UNDER ADIABATIC CONDITION

The present study investigated mass flow rate distribution and phase separation of R-22 in multi-microchannel tubes under adiabatic condition. The test section consisted of inlet and outlet headers with the inner diameter of 19.4 mm and 15 parallel multi-microchannel tubes. Each microchannel tube had 8 rectangular ports with hydraulic diameter of 1.32 mm. The key experimental parameters were the orientation of the header (horizontal and vertical), flow direction of refrigerant into the inlet header (in-line, parallel and cross flow), and inlet quality (0.1, 0.2, and 0.3). The effect of inlet quality on the mass flow rate distribution and phase separation in the microchannel tubes was negligible. The effect of the orientation of the header on the mass flow rate distribution and phase separation was the largest among the test parameters. Horizontal header showed better mass flow rate distribution and phase separation characteristics than vertical header. Both parallel and cross-flow conditions showed better mass flow rate distribution and phase separation than in-line flow condition.     

Two-Phase Flow Distribution to Tubes of Parallel Flow Air-Cooled Heat Exchangers

Abstract

This paper addresses two-phase flow distribution phenomena in multiple header–tube junctions used in heat exchangers. Because of phase separation, it is very difficult to obtain uniform two-phase flow distribution to the branch tubes. The flow distribution is strongly influenced by the header orientation (horizontal or vertical) and the number of branch tubes. Other factors that influence the flow distribution are the flow direction in the header (upflow or downflow), the header shape and tube end projection into the header, and the location and orientation of the inlet and exit connections. The source of maldistribution is the flow in the dividing headers. Work performed by the authors and others (including patents) are discussed. The possibilities for eliminating two-phase flow maldistribution are identified and discussed. This investigation shows that solutions, which provide uniform flow distribution, are very design-specific. Change of the geometry or operating parameters will require modification of the design.     

凝汽器水侧流动的三维数值模拟

建立了某一凝汽器实际管束的流动计算模型,运用计算流体力学的方法,对该凝汽器水侧流场进行了三维数值模拟。采用分区对称计算方法,大大降低网格数量,从而详细预测了凝汽器水侧进出口水室以及其连接管和冷却水管束内的流动特性。计算结果可以清楚地表明:该凝汽器进口水室存在大量漩涡,使流动阻力增加,流动恶化;水室速度分布不均匀,进口水室管板中心区域流体流速较高而边缘区域较低,结构上存在一定问题;而出口水室的结构较为合理。这与采用多孔介质模型模拟的结论一致,进一步验证了采用多孔介质模型对凝汽器进行计算是正确可行的。计算结果同时表明,冷却水管束内流量和流速的分布是不均匀的,位于中心位置的冷却水管流量较大,而周边区域较小,最大流量差别可达到38%,且相邻管路的流量减小幅度与冷却水管布置有关。冷却水管内冷却水流量和流速的差异将会影响换热器的换热性能。计算结果可为分析研究管排流动不均而引起的换热效率问题提供条件,也可为凝汽器设计和结构优化提供依据。     

电站锅炉再热器面积改变对过热器运行影响规律的研究

在对某发电厂200MW机组超温爆管进行的研究中发现,在尾部竖井中布置有分隔墙,低温过热器和低温再热器分别布置在分隔墙两侧,利用烟气挡板调节再热汽温的锅炉中,再热器面积的大小直接影响到过热器的运行情况。本文以该类型锅炉为研究对象,研究了再热器面积改变对过热器运行的影响规律,并提出通过适当养活再热器受热面来缓解过热器超温的思路。     

Distribution of air–water annular flow in a header of a parallel flow heat exchanger

The air and water flow distribution are experimentally studied for a heat exchanger composed of round headers and 10 flat tubes. The effects of tube protrusion depth as well as header mass flux, and quality are investigated, and the results are compared with previous 30 channel data. The flow at the header inlet is annular. For the downward flow configuration, water flow distribution is significantly affected by tube protrusion depth. For flush-mounted geometry, significant portion of water flows through frontal part of the header. As the protrusion depth increases, more water is forced to rear part of the header. The effect of header mass flux or quality is qualitatively the same as that of the protrusion depth. For the upward flow configuration, however, significant portion of water flows through rear part of the header. The effect of protrusion depth is the same as that of the downward flow. However, the effect of header mass flux or quality is opposite to the downward flow case. Compared with the previous 30 channel configuration, the present 10 channel configuration yields better flow distribution. Possible explanation is provided from flow visualization results.     

Double Perforated Impingement Plate in Shell-and-Tube Heat Exchanger

This article presents a solution to a chronic problem causing repeated tube failure at shell-and-tube heat exchangers. The problem is related to the fouling process on the tubes' surface, which accumulates downstream from the impingement plate at the exchanger inlet nozzle within the first tube rows due to low velocity and vortices production. In fouling services, the suspended deposits, fouling, accumulates on the tubes' surface downstream from the impingement plate, causing under-deposit corrosion, raising the tubes' surface temperature due to lack of cooling, and accelerating fouling process. Under-deposit corrosion attacks tubes and causes repeated tube failure, costing a lot of money in terms of material, maintenance, and production losses. Normal practice of extending tube life and delaying their failure is to upgrade the tubes' metallurgy. So the article objective is to present an economical solution option through modifying the impingement plate in the shell-and-tube heat exchangers where the impingement plate is recommended by the Tubular Exchanger Manufacturers Association (TEMA). The impingement modification is to replace the solid conventional impingement plate with double spaced plates having offset holes, called double perforated impingement plates (DPIP). The objective of this work can be met by comparing the simulation of the shell-side inlet flow distribution around the conventional and modified (DPIP) impingement plates and ensuring enhancement of the flow pattern distribution at the area behind the impingement plates. Since experimental work in flow investigation is time-consuming and costly, computational fluid dynamics (CFD) Fluent software was implemented as a cost-effective helpful tool to conduct the simulation for comparison purposes. The modified impingement plate, DPIP, will destroy vortices created behind the conventional plate, retarding fouling accumulation. DPIP will enhance shell-side flow distribution downstream from the impingement plate and will stop fouling accumulation on the tubes to prevent under-deposit corrosion.     

Effect of Two-Phase Natural Circulation Distortion on Tube Failure in Steam Boilers

Two different cases of evaporator tube ruptures in power station boilers due to natural circulation distortion are presented. The first case discussed concerns a 110-MW, unit boiler with bottom evaporation tubing inclined at 15° to the horizontal. At the high heat fluxes present in the furnace, subcooled boiling occurs in inclined tubes. For these inclinations an insufficient flow rate causes local heat transfer deficiencies due to vapor-water separation. The introduction of internally finned tubes eliminates local heat transfer deficiencies and prevents further tube failures. The second case is that of circulation interruption due to blowdown during start-up. The water level in the drum of this second 110-MW, unit boiler was controlled by inlet header blowdown during start-up. Thus, natural circulation was interrupted, causing local overheating of evaporator tubing. The event was identified by an increase of the tube rupture frequency. After changing the blowdown procedure, the interruptions of natural circulation were avoided and the tube failure frequency decreased substantially.     

Experimental investigation of the performance of an elbow-bend type heat exchanger with a water tube bank used as a heater or cooler in alpha-type Stirling machines

In this work the effect of the elbow-bend geometry and the effect of the tube arrangement on the performance of air-to-water heat exchanger is studied experimentally. In elbow-bend heat exchanger, the direction of the working fluid is bended at 90 degrees to its inlet direction. The heating or cooling fluid flows inside straight tubes while the working fluid flows past the tubes along an elbow pass. Three different types of the geometry of the elbow with three different tube bank arrangements were studied. The results were plotted and analyzed to clarify the effects of the elbow-bend geometry, the tube bank arrangements and the dead volume in the heat exchanger on the heat transfer and pressure drop. Two empirical correlations were deduced for each design, one to predict the relation between Nusselt and Reynolds numbers, while the other relation is between the friction factor and Reynolds number. This work was done to select the more suitable design to be used as a heater or a cooler in Stirling machines.