title: Ð§Ð¸ÑÐ»ÐµÐ½Ð½Ð¾Ðµ Ð¸ÑÑÐ»ÐµÐ´Ð¾Ð²Ð°Ð½Ð¸Ðµ ÑÐµÑÐµÐ½Ð¸Ñ Ð¸ ÑÐµÐ¿Ð»Ð¾Ð¾Ð±Ð¼ÐµÐ½Ð° Ð² Ð¾Ð´Ð½Ð¾ÑÑÐ´Ð½Ð¾Ð¼ Ð³Ð¾ÑÐ¸Ð·Ð¾Ð½ÑÐ°Ð»ÑÐ½Ð¾Ð¼ Ð¾ÑÐµÐ±ÑÐµÐ½Ð½Ð¾Ð¼ ÑÑÑÐ±Ð½Ð¾Ð¼ Ð¿ÑÑÐºÐµ Ð² ÑÐµÐ¶Ð¸Ð¼Ðµ ÑÐ²Ð¾Ð±Ð¾Ð´Ð½Ð¾Ð¹ ÐºÐ¾Ð½Ð²ÐµÐºÑÐ¸Ð¸
title: Ð²ÑÐ¿ÑÑÐºÐ½Ð°Ñ ÐºÐ²Ð°Ð»Ð¸ÑÐ¸ÐºÐ°ÑÐ¸Ð¾Ð½Ð½Ð°Ñ ÑÐ°Ð±Ð¾ÑÐ° Ð¼Ð°Ð³Ð¸ÑÑÑÐ°
titleType: Subtitle
title: Numerical simulation of free convection flow and heat transfer in a single-row horizontal finned tube bundle
Creators: name: Ð¤Ð¸Ð»Ð°ÑÐ¾Ð²Ð°, ÐÐ½Ð°ÑÑÐ°ÑÐ¸Ñ
Publisher: name: Ð¡Ð°Ð½ÐºÑ-ÐÐµÑÐµÑÐ±ÑÑÐ³ÑÐºÐ¸Ð¹ Ð¿Ð¾Ð»Ð¸ÑÐµÑÐ½Ð¸ÑÐµÑÐºÐ¸Ð¹ ÑÐ½Ð¸Ð²ÐµÑÑÐ¸ÑÐµÑ ÐÐµÑÑÐ° ÐÐµÐ»Ð¸ÐºÐ¾Ð³Ð¾
Year: 2024
Subjects: ÐÐ°ÑÐµÐ¼Ð°ÑÐ¸ÑÐµÑÐºÐ¾Ðµ Ð¼Ð¾Ð´ÐµÐ»Ð¸ÑÐ¾Ð²Ð°Ð½Ð¸Ðµ
Ð¿ÑÑÐºÐ¸ Ð¾ÑÐµÐ±ÑÐµÐ½Ð½ÑÑ ÑÑÑÐ±
Ð»Ð°Ð¼Ð¸Ð½Ð°ÑÐ½Ð¾Ðµ ÑÐµÑÐµÐ½Ð¸Ðµ
ÑÐ²Ð¾Ð±Ð¾Ð´Ð½Ð°Ñ ÐºÐ¾Ð½Ð²ÐµÐºÑÐ¸Ñ
Ð¸Ð½ÑÐµÐ½ÑÐ¸Ð²Ð½Ð¾ÑÑÑ ÑÐµÐ¿Ð»Ð¾Ð¾ÑÐ´Ð°ÑÐ¸
finned tube bundle heat exchanger
laminar flow
free convection
heat transfer intensity

description: ÐÑÐµÐ´ÑÑÐ°Ð²Ð»ÑÑÑÑÑ Ð´Ð°Ð½Ð½ÑÐµ ÑÐ²Ð¾Ð±Ð¾Ð´Ð½Ð¾ÐºÐ¾Ð½Ð²ÐµÐºÑÐ¸Ð²Ð½Ð¾Ð³Ð¾ ÑÐµÑÐµÐ½Ð¸Ñ Ð¸ ÑÐµÐ¿Ð»Ð¾Ð¾Ð±Ð¼ÐµÐ½Ð° Ð²Ð±Ð»Ð¸Ð·Ð¸ Ð¾Ð´Ð½Ð¾ÑÑÐ´Ð½Ð¾Ð³Ð¾ Ð¿ÑÑÐºÐ° Ð¸Ð· ÑÐµÑÑÐ¸ Ð½Ð°Ð³ÑÐµÑÑÑ Ð¾ÑÐµÐ±ÑÐµÐ½Ð½ÑÑ ÑÑÑÐ±. ÐÐ¾ÑÑÐ°Ð½Ð¾Ð²ÐºÐ° Ð·Ð°Ð´Ð°ÑÐ¸ Ð¿ÑÐ¸Ð±Ð»Ð¸Ð¶ÐµÐ½Ð° Ðº ÑÑÐ»Ð¾Ð²Ð¸ÑÐ¼ ÑÐºÑÐ¿ÐµÑÐ¸Ð¼ÐµÐ½ÑÐ°, ÑÐµÐ·ÑÐ»ÑÑÐ°ÑÑ ÐºÐ¾ÑÐ¾ÑÐ¾Ð³Ð¾ Ð¿ÑÐµÐ´ÑÑÐ°Ð²Ð»ÐµÐ½Ñ Ð² Ð´Ð¸ÑÑÐµÑÑÐ°ÑÐ¸Ð¸ ÐÐ°ÑÑÐ°Ð»Ð¾Ð²Ð¾Ð¹ Ð. Ð¡. (2019 Ð³.). Ð Ð°ÑÑÐ¼Ð¾ÑÑÐµÐ½Ñ Ð´Ð²Ðµ ÐºÐ¾Ð½ÑÐ¸Ð³ÑÑÐ°ÑÐ¸Ð¸ ÑÐ°ÑÑÐµÑÐ½Ð¾Ð¹ Ð¾Ð±Ð»Ð°ÑÑÐ¸: (1) Ð²ÐºÐ»ÑÑÐ°ÑÑÐ°Ñ Ð¿ÑÑÐ¾Ðº Ð¸Ð· ÑÐµÑÑÐ¸ Ð¾ÑÐµÐ±ÑÐµÐ½Ð½ÑÑ ÑÑÑÐ± Ð¸ (2) Ð¿ÐµÑÐ¸Ð¾Ð´Ð¸ÑÐµÑÐºÐ°Ñ, ÑÐ°ÑÐ°ÐºÑÐµÑÐ½Ð°Ñ Ð´Ð»Ñ Ð¿ÑÑÐºÐ° Ð¸Ð· Ð±ÐµÑÐºÐ¾Ð½ÐµÑÐ½Ð¾Ð³Ð¾ ÐºÐ¾Ð»Ð¸ÑÐµÑÑÐ²Ð° ÑÑÑÐ±. Ð ÑÐ¾Ð´Ðµ ÑÐ°ÑÑÐµÑÐ¾Ð² Ð²Ð°ÑÑÐ¸ÑÐ¾Ð²Ð°Ð»Ð¾ÑÑ ÑÐ°ÑÑÑÐ¾ÑÐ½Ð¸Ðµ Ð¼ÐµÐ¶Ð´Ñ ÑÑÑÐ±Ð°Ð¼Ð¸, Ð¾ÑÐ½Ð¾ÑÐ¸ÑÐµÐ»ÑÐ½Ð°Ñ (Ðº Ð´Ð¸Ð°Ð¼ÐµÑÑÑ ÑÐµÐ±ÑÐ°) Ð²ÐµÐ»Ð¸ÑÐ¸Ð½Ð° ÐºÐ¾ÑÐ¾ÑÐ¾Ð³Ð¾ Ð·Ð°Ð´Ð°Ð½Ð° ÑÐ°Ð²Ð½Ð¾Ð¹ Ï1 = 1.02â¦2.78. ÐÐ·ÑÑÐ°Ð»Ð¾ÑÑ ÑÐ°ÐºÐ¶Ðµ Ð²Ð»Ð¸ÑÐ½Ð¸Ðµ Ð·Ð½Ð°ÑÐµÐ½Ð¸Ñ ÑÐ¸ÑÐ»Ð° ÐÑÐ°ÑÐ³Ð¾ÑÐ° Gr, ÐºÐ¾ÑÐ¾ÑÐ¾Ðµ Ð²ÑÐ±Ð¸ÑÐ°Ð»Ð¾ÑÑ Ð¸Ð· Ð´Ð¸Ð°Ð¿Ð°Ð·Ð¾Ð½Ð° 3.9â104â¦5.6â105. ÐÐ¾Ð´ÐµÐ»Ð¸ÑÐ¾Ð²Ð°Ð½Ð¸Ðµ Ð¿ÑÐ¾Ð²Ð¾Ð´Ð¸Ð»Ð¾ÑÑ Ð² ÑÐ¾Ð¿ÑÑÐ¶ÐµÐ½Ð½Ð¾Ð¹ 3D Ð¿Ð¾ÑÑÐ°Ð½Ð¾Ð²ÐºÐµ Ð½Ð° Ð±Ð°Ð·Ðµ ÑÑÐ°Ð²Ð½ÐµÐ½Ð¸Ð¹ ÐÐ°Ð²ÑÐµ-Ð¡ÑÐ¾ÐºÑÐ° Ð¸ ÑÐ½ÐµÑÐ³Ð¸Ð¸. Ð§Ð¸ÑÐ»ÐµÐ½Ð½Ð¾Ðµ Ð¼Ð¾Ð´ÐµÐ»Ð¸ÑÐ¾Ð²Ð°Ð½Ð¸Ðµ Ð²ÑÐ¿Ð¾Ð»Ð½ÐµÐ½Ð¾ Ð² Ð¿Ð°ÐºÐµÑÐµ ANSYS Fluent. ÐÐ¾Ð´ÐµÐ»Ð¸ÑÐ¾Ð²Ð°Ð½Ð¸Ðµ ÑÐµÑÐµÐ½Ð¸Ñ Ð²Ð¾Ð·Ð´ÑÑÐ° Ð¾ÑÑÑÐµÑÑÐ²Ð»ÑÐ»Ð¾ÑÑ ÐºÐ°Ðº Ð² Ð¿ÑÐ¸Ð±Ð»Ð¸Ð¶ÐµÐ½Ð¸Ð¸ ÐÑÑÑÐ¸Ð½ÐµÑÐºÐ° Ð´Ð»Ñ ÑÑÐµÑÐ° ÑÑÑÐµÐºÑÐ¾Ð² Ð¿Ð»Ð°Ð²ÑÑÐµÑÑÐ¸, ÑÐ°Ðº Ð¸ Ð½Ð° Ð¾ÑÐ½Ð¾Ð²Ðµ Ð¼Ð¾Ð´ÐµÐ»Ð¸ ÑÐ¶Ð¸Ð¼Ð°ÐµÐ¼Ð¾Ð³Ð¾ ÑÐ¾Ð²ÐµÑÑÐµÐ½Ð½Ð¾Ð³Ð¾ Ð³Ð°Ð·Ð° Ñ Ð¿ÐµÑÐµÐ¼ÐµÐ½Ð½ÑÐ¼Ð¸ ÐºÐ¾ÑÑÑÐ¸ÑÐ¸ÐµÐ½ÑÐ°Ð¼Ð¸ Ð´Ð¸ÑÑÑÐ·Ð¸Ð¾Ð½Ð½Ð¾Ð³Ð¾ Ð¿ÐµÑÐµÐ½Ð¾ÑÐ°. ÐÐ¾Ð»ÑÑÐµÐ½Ð½ÑÐµ Ð´Ð°Ð½Ð½ÑÐµ Ð¾ ÑÐµÐ¿Ð»Ð¾Ð¾ÑÐ´Ð°ÑÐµ (ÑÑÐµÐ´Ð½ÐµÐ¼ Ð·Ð½Ð°ÑÐµÐ½Ð¸Ð¸ ÑÐ¸ÑÐ»Ð° ÐÑÑÑÐµÐ»ÑÑÐ° Nu) Ð² Ð¿Ð¾ÑÑÐ°Ð½Ð¾Ð²ÐºÐ°Ñ (1) Ð¸ (2) ÐºÐ°ÑÐµÑÑÐ²ÐµÐ½Ð½Ð¾ Ð¸ ÐºÐ¾Ð»Ð¸ÑÐµÑÑÐ²ÐµÐ½Ð½Ð¾ ÑÐ¾Ð³Ð»Ð°ÑÑÑÑÑÑ ÐºÐ°Ðº Ð¼ÐµÐ¶Ð´Ñ ÑÐ¾Ð±Ð¾Ð¹, ÑÐ°Ðº Ð¸ Ñ Ð´Ð°Ð½Ð½ÑÐ¼Ð¸ ÑÐºÑÐ¿ÐµÑÐ¸Ð¼ÐµÐ½ÑÐ¾Ð² Ð² ÑÐ°ÑÑÐ¼Ð¾ÑÑÐµÐ½Ð½Ð¾Ð¼ Ð´Ð¸Ð°Ð¿Ð°Ð·Ð¾Ð½Ðµ Gr. ÐÐ¾ÐºÐ°Ð·Ð°Ð½Ð¾, ÑÑÐ¾ Ð¿ÑÐ¸ ÑÐ²ÐµÐ»Ð¸ÑÐµÐ½Ð¸Ð¸ Ð¼ÐµÐ¶ÑÑÑÐ±Ð½Ð¾Ð³Ð¾ ÑÐ°ÑÑÑÐ¾ÑÐ½Ð¸Ñ Ð¸Ð½ÑÐµÐ½ÑÐ¸Ð²Ð½Ð¾ÑÑÑ ÑÐµÐ¿Ð»Ð¾ÑÑÐµÐ¼Ð° Ñ Ð¿Ð¾Ð²ÐµÑÑÐ½Ð¾ÑÑÐ¸ Ð²ÑÐµÑ ÑÑÑÐ± Ð²Ð¾Ð·ÑÐ°ÑÑÐ°ÐµÑ, Ð´Ð¾ÑÑÐ¸Ð³Ð°Ñ Ð¼Ð°ÐºÑÐ¸Ð¼Ð°Ð»ÑÐ½Ð¾Ð³Ð¾ (Ð¾Ð¿ÑÐ¸Ð¼Ð°Ð»ÑÐ½Ð¾Ð³Ð¾) Ð·Ð½Ð°ÑÐµÐ½Ð¸Ñ. ÐÐ¿ÑÐ¸Ð¼Ð°Ð»ÑÐ½Ð¾Ðµ ÑÐ°ÑÑÑÐ¾ÑÐ½Ð¸Ðµ Ð´Ð»Ñ Ð¼Ð°ÐºÑÐ¸Ð¼Ð°Ð»ÑÐ½Ð¾Ð³Ð¾ Gr ÑÐ¾Ð¾ÑÐ²ÐµÑÑÑÐ²Ð¾Ð²Ð°Ð»Ð¾ Ï1 = 1.11, Ð° Ð´Ð»Ñ Ð¼Ð¸Ð½Ð¸Ð¼Ð°Ð»ÑÐ½Ð¾Ð³Ð¾ â Ï1 = 1.26. ÐÐ°Ð»ÑÐ½ÐµÐ¹ÑÐµÐµ ÑÐ²ÐµÐ»Ð¸ÑÐµÐ½Ð¸Ðµ Ð·Ð°Ð·Ð¾ÑÐ° Ð¼ÐµÐ¶Ð´Ñ ÑÑÑÐ±Ð°Ð¼Ð¸ ÑÐ¾Ð¿ÑÐ¾Ð²Ð¾Ð¶Ð´Ð°ÐµÑÑÑ Ð¿Ð¾ÑÑÐµÐ¿ÐµÐ½Ð½ÑÐ¼ ÑÐ¼ÐµÐ½ÑÑÐµÐ½Ð¸ÐµÐ¼ ÑÐµÐ¿Ð»Ð¾Ð¾ÑÐ´Ð°ÑÐ¸. ÐÐ¾Ð»ÑÑÐµÐ½Ñ ÑÐµÑÑÑÐµ Ð±Ð°Ð·Ñ Ð´Ð°Ð½Ð½ÑÑ, ÑÑÐ¼Ð¼Ð°ÑÐ½Ð¾ ÑÐ¾ÑÑÐ¾ÑÑÐ¸Ðµ Ð¸Ð· 5000 Ð²Ð°ÑÐ¸Ð°Ð½ÑÐ¾Ð², Ð½Ð° Ð¾ÑÐ½Ð¾Ð²Ðµ ÐºÐ¾ÑÐ¾ÑÑÑ Ð¾Ð¿ÑÐµÐ´ÐµÐ»ÐµÐ½Ñ ÐºÐ¾ÑÑÐµÐ»ÑÑÐ¸Ð¾Ð½Ð½ÑÐµ Ð·Ð°Ð²Ð¸ÑÐ¸Ð¼Ð¾ÑÑÐ¸ Nu Ð¾Ñ Gr Ð¸ Ï1.
description: Data are presented on free convective flow and heat transfer near a single-row bundle of six horizontal oriented heated tubes. The formulation of the problem is close to the experimental conditions, which results were presented in the dissertation by Marshalova G. S. (2019). Two configurations of the computational domain are considered: (1) including a bundle of six finned tubes and (2) periodic, for a bundle of infinite number of tubes. During calculations, the distances between the pipes were varied, the relative (to the fin diameter) value of which was set equal to Ï_1Â  = 1.02â¦2.78. In addition, the influence of the Grashof number value, which was selected from the range Gr = 3.9â10^4Â  â¦5.6â10^5, was studied. The simulations have been carried out in a conjugate 3D formulation using the Navier-Stokes and energy equations. Numerical simulations have been performed in the ANSYS Fluent package. Modeling of air flow has been carried out both: in the Boussinesq approximation for the effects of buoyancy, and a model of a compressible perfect gas with variable diffusion transfer coefficients. The obtained data on heat transfer (the average value of the Nusselt number Nu) in formulations (1) and (2) are qualitatively and quantitatively consistent with each other and with the experimental data in the considered range of Gr. It is shown that as the distance between pipes increases, the intensity of heat removal from the surface of all pipes increases, reaching a maximum (optimal) value. The optimal distance for the maximum Gr corresponded to Ï_1Â  = 1.11, and for the minimum â Ï_1Â  = 1.26. A further increase in the gap between the pipes is accompanied by a gradual decrease in heat transfer. Four databases have been obtained, consisting of a total of 5000 options, on the basis of which the correlation dependences of Nu on Gr and Ï_1 were determined.