秦山核电二期工程蒸汽发生器的设计特点

本文介绍了秦山核电二期工程２×６００ＭＷ的５５／１９Ｃ型蒸汽发生器所具有的主要特点，以及所用传热管材、管径的选取．设计中采用了带直段的过渡锥壳、液压胀管等技术，易于在役检查和运行维修工作．     

煤氧喷枪中心氧管参数之间的关系

利用等截面管中氧气射流理论公式对影响煤氧喷枪中心氧管氧气流动的主要参数进行计算。计算结果表明：氧气出口马赫数及氧气入口压力与氧管内径、氧气流量、炉内操作压力以及氧气入口温度等因素有关。同时推出计算氧气出口马赫数和氧气入口压力的显式函数公式：Ｍ２＝Ｑ＾０．８９６３９Ｔ１＾０．４２４８５／ｐ３＾０．８７３３４Ｄ＾１．８２７１２×４．３４００７×１０＾－８ ｐ１＝Ｔ１＾０．４９１７９ｐ３＾０．１３６８１     

Results of long-term operation of cascade tubular air heaters at the Berezovskaya GRÉS

Experience of operation of tubular air heaters (TAH) on twelve boilers of type PK-38 for 150-MW power units of the Berezovskaya GRÉS (state regional power plant) in Belarus is presented. Coal-fired, gas-fired, and oil-fired operation modes with updating tubular air heaters in a cascade layout are described. Advantages of the cascade layout and conditions for reliable, efficient, and long-term service of the TAH are shown.Translated from Élektricheskie Stantsii, No. 9, September 2004, pp. 20–23.     

催化裂化余热锅炉省煤器的改进

针对重油催化裂化余热锅炉省煤器经常"爆管"而难以运行的问题,分析原因后提出三种改进方 案,并优选一种方案实施,成功地解决了该问题,同时大幅度提高了锅炉过热蒸汽产量,节能效果显著。     

常减压蒸馏装置常顶换热器腐蚀原因分析及预防

中国石化股份有限公司天津分公司常减压蒸馏(Ⅱ)套装置的常顶换热器管束,自2003年8月份以来多次发生腐蚀泄漏。经调查,由于电脱盐装置的脱盐合格率仅为14.5％,因此塔顶馏分油中的H2S,HCl和管板焊缝部位焊接应力共同作用,导致了管板焊缝发生了应力腐蚀。加强"一脱三注"管理,管内涂覆涂料以及选用09Cr2A1MoRe或RT360材质的管束可预防腐蚀泄漏的发生。     

A general steady state mathematical model for fin-and-tube heat exchanger based on graph theory

Fin-and-tube heat exchangers are widely used in air conditioners, chillers, etc. A lot of factors, including arrangement of refrigerant circuits, configure specification of fins and tubes, and operating conditions, have significant influence on the performance of fin-and-tube heat exchangers. For the purpose of fast design of high performance heat exchangers, a simulator reflecting the influence of these factors is necessary. In this paper, a general steady state mathematic model based on the graph theory is presented. With the help of the directed graph and graph-based traversal methods (Breadth-first search and Depth-first search), this model is capable to describe any flexible refrigerant circuit arrangement, and quantify the refrigerant distribution in the refrigerant circuit and heat conduction through fins. An alternative iteration method is also developed to solve the conservation equations, which can shorten the simulating time effectively. The model is verified with the experimental results, and the maximum error is within ±10.0%. A simulator based on this model has been used for designing practical fin-and-tube heat exchangers.     

Flow condensation heat transfer coefficients of R22, R134a, R407C, and R410A inside plain and microfin tubes

Flow condensation heat transfer coefficients (HTCs) of R22, R134a, R407C, and R410A inside horizontal plain and microfin tubes of 9.52 mm outside diameter and 1 m length were measured at the condensation temperature of 40 °C with mass fluxes of 100, 200, and 300 kg m⁻² s⁻¹ and a heat flux of 7.7–7.9 kW m⁻². For a plain tube, HTCs of R134a and R410A were similar to those of R22 while HTCs of R407C are 11–15% lower than those of R22. For a microfin tube, HTCs of R134a were similar to those of R22 while HTCs of R407C and R410A were 23–53% and 10–21% lower than those of R22. For a plain tube, our correlation agreed well with the present data for all refrigerants exhibiting a mean deviation of 11.6%. Finally, HTCs of a microfin tube were 2–3 times higher than those of a plain tube and the heat transfer enhancement factor decreased as the mass flux increased for all refrigerants tested.     

加热炉炉管的红外热像监测方法研究

文中所介绍的乃是获奖项目“高温炉管的红外在线监测诊断及评估系统研究”科研成 果的一部分。试验研究结果表明,在进口的如PM350 类焦平面红外热像仪的基础上,合理地选装高温火焰滤片、广角镜头以及红外隔热罩,便可实现通过看火孔对加热炉炉管进行红外热像的在线监测。而通过试验研究所得到的误差修正方法,可以使炉管的红外热像监测结果与接触式的热电偶测试结果相差小于2 %。现场工业试验的结果表明,该方法完全满足了生产装置监测的需要。     

Evaluation of thermal contact conductance using a new experimental-numerical method in fin-tube heat exchangers

In a fin-tube heat exchanger the contact between fin collar and tube surface is obtained through mechanical expansion of tubes. Since the interfaces between the tubes and fins consist partially of metal-to-metal contact and partially of air, the features of heat transfer through the contact interfaces have not been fully investigated. The present study aims at the development of a new tool including an experiment and a numerical calculation for the estimation of the thermal contact conductance between the fin collar and tube surface, and pursues the evaluation of the factors affecting the thermal contact conductance in a fin-tube heat exchanger. Heat exchangers fabricated for the current study have been put to the test for heat balance in a vacuum chamber with water as an internal fluid. And a finite difference numerical scheme has been used for the data reduction of the experimental data to evaluate the thermal contact conductance. Fin-tube heat exchangers employed in the current research are of tube diameter of 7 mm with different tube expansion ratios, fin spacings, and fin types. The results of the present study imply that these parameters as well as hydrophilic fin coating have a significant effect on the thermal contact conductance. It has been discovered that the portion of the thermal contact resistance is not negligible compared with the total thermal resistance in a fin-tube heat exchanger, and this means that in order to reduce the thermal contact resistance thoughtful care should be taken in fabricating heat exchangers.     

Measurement of spray boiling refrigerant coefficients in an integral-fin tube bundle segment simulating a full bundle

Outside (refrigerant) boiling coefficients for a combination of spray and drip boiling for a low pressure refrigerant have been obtained from overall heat transfer coefficients in a 1024 fins per meter tube bundle segment. The tubes were heated by water on the inside; liquid refrigerant was sprayed and/or dripped on the outside. Also, refrigerant vapor was supplied at the bottom of the bundle segment. This configuration simulates an actual flooded evaporator under spray boiling conditions. The dripping corresponds to liquid film falling from upper rows while the inlet vapor is equivalent to the vaporized refrigerant rising from lower tubes; the refrigerant vapor can influence heat transfer performance by the combined effects of gas convection and liquid shear on the tubes. For a nominal heat flux of 23,975 W/m², a bundle average outside heat transfer coefficient of 8522 W/m² °C, based on nominal tube outer diameter, was found at an average bundle vapor mass flux equal to 12.4 kg/s m². The distributor plate below the bundle enhanced the heat transfer, especially at lower vapor mass fluxes, by providing a level of liquid hold-up just below the bottom tube row.